Through-flow component and method for treating a fluid

Abstract

A through-flow component (10) is provided for mixing at least one first volume flow and one second volume flow. The through-flow component comprises a main body (20) and a mixing structure (30) arranged within the main body. The first volume flow and the second volume flow flow through the main body in a flow direction. The mixing structure has a plurality of structure elements (40), wherein the plurality of structure elements are in at least partial fluidic contact with at least one of volume flows, the first volume flow or the second volume flow, and wherein at least two of the structure elements are arranged along an inner circumferential direction of the main body.

Description

-1- Description Title: _ FLOW-THROUGH COMPONENT, SYSTEM AND METHOD FOR THE TREATMENT OF A FLUID CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims priority to Luxembourg patent application LU 503245, filed on December 22, 2022. The entire disclosure of Luxembourg patent application LU 503245 is hereby incorporated by reference. TECHNICAL FIELD OF THE INVENTION

[0002] The invention relates to a flow-through component for mixing volume flows, a system and a method for treating a fluid and a computer-implemented method for controlling the system. BACKGROUND OF THE INVENTION

[0003] Currently established wastewater treatment methods can be divided into two groups. The first group of processes merely separates the substances to be disposed of or problematic substances and requires further downstream processing steps for their mineralization. Examples of material separation processes such as flotation, filtration, sedimentation, reverse osmosis, and evaporation only result in partial disposal of the substances to be disposed of. The concentrates and sludges resulting from these processes must be permanently disposed of in hazardous waste landfills or by incineration.

[0004] A second group of processes consists of oxidation processes, such as the technically implemented processes of ozonation, UV / hydrogen peroxide, UV / iron catalyst / hydrogen peroxide, the Fenton process with an iron catalyst and hydrogen peroxide, or the ORC AN process with hydrogen peroxide / iron catalyst and atmospheric oxygen. These processes transform the substances to be disposed of into a biocompatible form or oxidize the substances to be disposed of directly to CO2 and water. -2- use auto-oxidation processes that differ significantly in their efficiency due to the specific process conditions.

[0005] High-temperature wet incineration, which operates primarily with pure oxygen at temperatures of 200 to 280 °C, has gained technical significance among the oxidation processes for the disposal of organic wastewater constituents, such as the Krupp-KATOX process. Another oxidation process is the LOPROX process, which, unlike the Krupp-KATOX process, is a low-pressure process. Typical operating conditions for low-pressure processes are pressures of 5 to 20 bar and temperatures below 200 °C. Other low-pressure processes operate at pressures between 1 and 5 bar and temperatures in the range of 100 to 150 °C with free-radical oxidants, preferably hydrogen peroxide.

[0006] The aforementioned high-temperature and low-pressure processes usually operate under cost-intensive operating conditions and require expensive corrosion-resistant steels and materials. UV-based low-pressure processes (e.g., UV / H2O2, UV / O3, UV / catalyst) have a limited reaction temperature of < 60 °C, are only applicable to particle- and solids-free and transparent wastewater, and achieve a low space-time yield compared to other oxidation processes. Ozone-based processes (e.g., O3, O3 / H2O2, O3 / catalyst) operate at low temperatures of < 40 °C and, due to their high energy consumption, incur high operating costs with a low space-time yield.Fenton-based processes (e.g., Fenton, Photo / Fenton) feature low operating temperatures of primarily 60 °C, require high catalyst concentrations of 10 mmol / L and higher of an iron salt, have a limited pH range of < 3.0, and long reaction times of up to several hours, resulting in comparatively high operating and investment costs. Modified Fenton-based processes operated with atmospheric oxygen demonstrate higher efficiency at lower operating costs. However, these processes also have a limited pH range of < 3.0 due to the use of an iron catalyst, as well as limited air mixing in the jet stream despite a jet pipe installed above a nozzle. This results in a higher consumption of hydrogen peroxide, combined with a decreasing oxidation efficiency with increasing chemical oxygen demand (CS O concentration) in the reactor outlet. -3-

[0007] The oxidation processes mentioned above also have limited applicability due to phase separation that occurs in the reactor during the oxidative mineralization of emulsions and dispersions.

[0008] EP 0 937 011 B1 describes a process for the oxidation of wastewater constituents, as well as a nozzle system and a plant for carrying it out. The core of the process is the superposition of three radical chain cycles to form a continuously running reaction chain, which is maintained by incorporating a radical initiator, catalyst, and oxygen into the wastewater stream. Of central importance in terms of reaction technology is the combination of the reactants via a nozzle system, which is characterized by the formation of unsteady flow conditions. The nozzle system comprises a reaction nozzle, which is preferably designed as a rotationally symmetrical multiple Laval nozzle.

[0009] EP 2 791 067 B1 describes a process for the oxidation of contaminated wastewater, a plant for carrying out the process, and a device, in particular a nozzle, for treating wastewater. The nozzle has an outer tube and an inner tube, with an intermediate space being formed between the outer tube and the inner tube. The intermediate space between the outer tube and the inner tube is divided into at least two chambers in the longitudinal direction of the tubes, with the inner tube tapering and widening again in the longitudinal direction, and the inner tube having at least one opening into each chamber at the tapered point. The nozzle is preferably designed to be rotationally symmetrical.

[0010] However, the prior art does not disclose a system or method for improving the efficiency of the oxidation of substances to be disposed of by better mixing of the volume flows involved in the oxidation. SUMMARY OF THE INVENTION

[0011] The invention is based on the technical problem of providing an improved oxidation process for the disposal of substances with better mixing of the volume flows involved in the oxidation.

[0012] This technical problem is solved by a flow-through component for mixing volume flows, a system and a method for treating a fluid, and a computer-implemented method for controlling the system. -4- This document describes a flow-through component for mixing at least a first volume flow and a second volume flow. The flow-through component comprises a base body through which the first volume flow and the second volume flow flow in one flow direction, as well as a mixing structure arranged within the base body with a plurality of structural elements. The plurality of structural elements are at least partially in fluidic contact with at least one of the first volume flow and the second volume flow. At least two of the structural elements are arranged along an inner circumferential direction of the base body.

[0013] The mixing structure generates highly dynamic turbulence in the flow component, leading to improved mixing of the first volume flow and the second volume flow. Cavitation effects within the flow component triggered by the mixing structure lead to an increase in the interface between the phases of the first volume flow and the second volume flow, thus increasing radical formation.

[0014] In addition, at least two of the structural elements can be arranged along the flow direction, and the structural elements can be arranged at least partially in a spiral shape along the flow direction. This further promotes the generation of highly dynamic turbulence and cavitation effects.

[0015] The structural elements can be arranged, at least partially, along the flow direction in at least one of a left-handed spiral and a right-handed spiral, and the winding ratios of the left-handed spiral and / or the right-handed spiral can correspond to Fibonacci numbers. This further promotes the generation of highly dynamic turbulence and cavitation effects.

[0016] The base body can have at least one or more of a cylindrical, conical, hyperbolic, and double-conical shape along the flow direction, and at least one of the structural elements can have a tetrahedral, parabolic, conical, and pyramidal shape. This further promotes the generation of highly dynamic turbulence and cavitation effects.

[0017] The mixed structure can at least partially comprise a catalyst compound. This allows a heterogeneously catalyzed reaction to be carried out. -5-

[0018] Furthermore, a system for treating a fluid is described. The system comprises a reactor and a flow-through component according to the invention arranged on the reactor. The system further comprises a nozzle device configured to supply at least a first volume flow and a second volume flow into the flow-through component.

[0019] The nozzle device may comprise a multi-component nozzle and the reactor may comprise an inner body for generating a reactor-intrinsic recirculation flow, wherein the flow-through component may be arranged at least partially within the inner body.

[0020] The system may further comprise a separation device for separating a phase from the reactor, wherein the separation device may comprise at least one of a ring line, an overflow edge or a float, and wherein the separation device may comprise a suction pump for sucking the phase and returning the phase by means of the nozzle device to the flow-through component and / or discharging the phase.

[0021] Furthermore, a method for treating a fluid in a reactor with a flow-through component according to the invention is described. The method comprises the steps of feeding at least a first volume flow and a second volume flow into the flow-through component by means of a nozzle device and mixing the first volume flow and the second volume flow within the flow-through component to promote a reaction chain between the first volume flow and the second volume flow.

[0022] The method may further comprise the steps of separating a phase from the reactor by means of a separation device, returning the separated phase to the flow-through component by means of the nozzle device and / or removing the separated phase.

[0023] Furthermore, a computer-implemented method for controlling a system for treating a fluid in a reactor with a flow-through component is described. The computer-implemented method comprises the steps of detecting an actual value of at least one target variable of the system using a sensor, determining a control value of at least one control variable from the actual value of the target variable, a target value of the target variable, and an actual value of the control variable using an optimization algorithm, and -6- Setting the control variable to the control value by means of a control device included in the system.

[0024] The optimization algorithm can be a gradient descent optimization algorithm or an evolutionary optimization algorithm. At least one target variable can also be a technical or commercial parameter.

[0025] The at least one control variable can be, for example, the pH value of the fluid treated by the system or a dosage value for peroxide, air or catalyst supplied to the system.

[0026] The at least one target variable can preferably be the chemical oxygen demand (COD concentration), preferably the color or preferably the AOX concentration (adsorbable organic bound halogens) of the fluid supplied to the system or of the fluid currently contained in the system.

[0027] A computer program is also described. The computer program comprises instructions which, when executed by a computer, cause the computer to execute the computer-implemented method according to the invention.

[0028] Furthermore, a computer-readable medium is described. The computer-readable medium comprises instructions which, when executed by a computer, cause the computer to execute the computer-implemented method according to the invention. BRIEF DESCRIPTION OF THE CHARACTERS

[0029] Fig. 1 shows a system for treating a fluid according to a first aspect.

[0030] Fig. 2 shows a system for treating a fluid according to a second aspect.

[0031] Fig. 3 A shows a perspective view of a flow-through component according to a first aspect.

[0032] Fig. 3B shows a sectional view of the flow-through component according to the first aspect.

[0033] Fig. 3C shows a perspective view of the negative form of a mixing structure of the flow-through component according to the first aspect.

[0034] Fig. 3D shows another sectional view of the flow-through component according to the first aspect. -7-

[0035] Fig. 3E shows a perspective sectional view of the flow-through component according to the first aspect.

[0036] Fig. 4A-D show different shapes of structural elements of the flow-through component.

[0037] Fig. 5A-D show different shapes of base bodies of the flow-through component.

[0038] Fig. 6A shows a plan view of a nozzle device.

[0039] Fig. 6B shows a sectional view of the nozzle device.

[0040] Fig. 7A shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a first example with the system according to the invention.

[0041] Fig. 7B shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to the first example without the system according to the invention.

[0042] Fig. 8A shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a second example with the system according to the invention.

[0043] Fig. 8B shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to the second example without the system according to the invention.

[0044] Fig.9 shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a third example with the system according to the invention.

[0045] Fig. 10 shows a flow diagram of a method according to the invention for treating a fluid.

[0046] Fig. 11 shows a flowchart of a computer-implemented method according to the invention for controlling the system according to the invention. DETAILED DESCRIPTION OF THE INVENTION

[0047] The invention will now be described based on the drawings. It is understood that the embodiments and aspects of the invention described herein are only examples and do not limit the scope of the claims in any way. The invention is defined by the claims and their equivalents. It is understood that features of one aspect or embodiment of the invention may be combined with a feature of another aspect or other aspects and / or embodiments of the invention. -8-

[0048] Fig. 1 shows a system 70 for treating a fluid according to a first aspect. The system 70 comprises a reactor 75 with a reactor diameter DR, a flow-through component 10 or booster tube, and a nozzle device 80. The reactor can, for example, consist of a closed vessel. The reactor 75 can have one or more removable and reattachable parts, such as a lid at the upper end of the reactor 75 and / or a base part at the lower end of the reactor 75. The flow-through component 10 and the nozzle device 80 together form a nozzle-booster system. The flow-through component 10 is arranged within the reactor 75, preferably at the bottom. The nozzle device 80 is arranged in line or flush with the flow-through component 10. The nozzle device is directly adjacent to the flow-through component 10 in the direction of flow RI.can be arranged offset by several diameters of the through-flow component 10 in the direction of flow RI from the through-flow component 10. The through-flow component 10 is designed to be arranged in the reactor 75 so as to be interchangeable depending on the medium of the fluid. The through-flow component 10 is designed not to be permanently connected to the nozzle device 80 in the reactor 75. In particular, the through-flow component 10 is detachably connected to the nozzle device 80 so as to be interchangeable depending on the medium. Since the through-flow component 10 is not permanently connected to the nozzle device 80, the nozzle device 80, in particular the nozzle device 80 designed as a multi-component nozzle with external mixing 86, and the through-flow component 10 can operate independently of one another.

[0049] The system 70 further comprises an inner body 90 arranged within the reactor 75. The flow-through component 10 is arranged at least partially within the inner body 90. The nozzle device 80 can also be arranged at least partially within the inner body. The inner body 90 can be tubular with a circular or oval cross-section, for example, and serves to generate a reactor-intrinsic recirculation flow 95.

[0050] The nozzle device 80 serves to supply one or more volume flows VI to V4 or fluids into the reactor 75. The nozzle device 80 is described in detail with Fig. 6A and 6B. The nozzle device 80 is connected to one or more volume flows VI to V4 and can supply them to the reactor 75 such that the supplied volume flows VI to V4 flow through the flow component 10. The -9- Volume flows VI to V4 are mixed as they flow through the flow component 10.

[0051] A first volume flow V1 is supplied to the nozzle device 80 via a circulation pump 110. The first volume flow VI is, for example, a fluid to be treated by the system 70, such as organically contaminated wastewater. The first volume flow VI represents the supply of the wastewater to the system 70. The first volume flow VI is supplied to the reactor 75 via the nozzle device 80 and flows through the flow-through component 10.

[0052] A second volume flow V2 is also supplied to the nozzle device 80. The second volume flow V2 is air, pure oxygen, or an oxygen-containing gas. The second volume flow V2 is supplied to the reactor 75 via the nozzle device 80 and flows through the flow-through component 10. The second volume flow V2 can be supplied to the nozzle device 80 via a pump.

[0053] A third volume flow V3 is also supplied to the nozzle device 80. The third volume flow V3 is a free-radical-forming oxidizing agent, preferably hydrogen peroxide. The third volume flow V3 is supplied to the reactor 75 via the nozzle device 80 and flows through the flow-through component 10. The third volume flow V3 can be supplied to the nozzle device 80 via a pump.

[0054] A fourth volume flow V4 is also fed to the nozzle device 80. The fourth volume flow V4 is a catalyst for operating the reactor 75 with homogeneous catalysis, for example a catalyst or a mixture of salts of transition metals or an organic quinoid / benzenoid compound system. The use of organic catalysts with a quinoid / benzenoid structure, such as 1,4-benzoquinone and anthraquinone, finds its application in the pH range from 5 to 11, preferably in the range from 6 to 10. The fourth volume flow V4 is fed to the reactor 75 by means of the nozzle device 80 and flows through the flow-through component 10. The fourth volume flow V4 can be fed to the nozzle device 80 by means of a pump.

[0055] A fifth volume flow V5 is withdrawn from the reactor via a discharge line. The fifth volume flow V5 can, for example, remove remaining residues from reactor 75. -10-

[0056] Furthermore, a circulation volume flow can be withdrawn from the reactor 75 via a circulation line 115 and fed back to the reactor 75 via the circulation pump 110 and the nozzle device 80. Thus, wastewater already present in the reactor 75 can flow through the flow-through component 10 again.

[0057] Individual volume flows described may be omitted. Not all of the described volume flows necessarily have to flow through the flow-through component 80. Likewise, not all of the described volume flows have to be supplied to the reactor 75 via the nozzle device 80, but can also be supplied to the reactor 75 in other ways. Some of the described volume flows can also be mixed upstream of the nozzle device 80 and can be supplied together to the nozzle device 80. The described volume flows can be completely unmixed or already partially mixed upon entering the flow-through component 10.

[0058] The system 70 also includes a shower 120, consisting of a shower line and a spray nozzle located in an upper part of the reactor 75. The shower 120 can also be used to treat foaming media without disruption. The spray nozzle of the shower 120 is fed by a specially installed pump and has a flow rate of 10 to 50 L / min, depending on the volume of the reactor 75.

[0059] The system 70 also includes an exhaust air discharge 130 arranged in an upper part of the reactor 75 for discharging gases during operation of the reactor 75.

[0060] The system 70 further comprises a separation device 100 for separating a water-insoluble phase, such as an oil phase, forming in the reactor 75 on the surface of a fluid present in the reactor, and for removing the separated oil phase from the reactor 75. Separation and removal of the oil phase may be necessary, particularly due to the multiphase nature of various wastewaters (e.g., emulsions and oil-containing dispersions). Emulsions and dispersions are predominantly thermodynamically unstable systems that decompose into individual mixed phases at elevated temperatures (< 60 °C). The separation device 100 adaptively adjusts to the level of the supernatant phase in order to remove only the supernatant phase.

[0061] The separation device 100 comprises an overflow edge 102, in particular a flexible overflow edge 102, for separating the oil phase and a suction pump 106 for -11- Suction or separation of the oil phase from the reactor 75. Instead of the overflow edge 102, the separation device 100 can also comprise a ring line, in particular a flexible ring line. The suction pump 106 is configured to suction the floating phase and return the floating phase to the flow-through component 10 via the multi-component nozzle with external mixing 86. Furthermore, the suction pump 106 can be configured to discharge the floating phase.

[0062] The separated and separated oil phase can either be removed from the system 70 and permanently disposed of, for example, in hazardous waste landfills or by incineration. This can be particularly effective for separated non-oxidizable oils such as perfluorinated hydrocarbons. Alternatively, the separated and separated oil phase can be returned to the reactor 75, as can be effective, for example, for separated oxidizable oils. The return can be effected, for example, by means of the suction pump 106 via the circulation line and the nozzle device 80.

[0063] The system further comprises a processor 150, which is connected to a sensor S or a measuring device and at least one control device SV. The processor 150 can communicate with the sensor S and the at least one control device SV either by wired communication and / or by wireless communication. The processor can be arranged on the reactor 75 or separately from the reactor 75. The sensor S is arranged in the reactor 75 and is configured to detect the chemical oxygen demand (C SB concentration) of the fluid currently contained in the system 70. Alternatively, the sensor S can detect the chemical oxygen demand of the first volume flow VI supplied to the system 70.

[0064] The at least one control device SV is arranged in a supply line of the second volume flow V2, the third volume flow V3, and / or the fourth volume flow V4 and is configured to meter the amount of the respective volume flow supplied to the reactor 75. The control device SV can, for example, be an electrically controllable valve. The circulation pump 110 can also represent a control device SV, by means of which the amount of the first volume flow 75 supplied to the reactor can be adjusted.

[0065] The system 70 is used to carry out an oxidation process for the disposal of organically contaminated wastewater (first volume flow VI) in the reactor 75 with -12- Feeding of a radical starter (third volume flow V3), a catalyst (fourth volume flow V4) and an oxygen-containing gas (second volume flow V2) into a hydrodynamic, highly turbulent jet flow.

[0066] The flow-through component 10 plays an important role in the efficiency of the oxidation process carried out with the system 70. The flow-through component 10 is described in detail with Figs. 3 A - 3E. The volume flows VI, V2, V3 and V4 are mixed as they flow through the flow-through component 10 by generating highly dynamic turbulence. Pronounced cavitation effects within the flow-through component 10 lead to the increased formation of micro-droplets and thus to an increase in the interface between the liquid and gas phases of the mixed volume flow. The oxidation of the organic wastewater constituents preferentially takes place at the phase boundaries, which is why the increase in the interface between the liquid and gas phases leads to increased radical formation, particularly OH* radicals, and consequently to higher degradation rates of the organic wastewater constituents.

[0067] By using a flow-through component 10 in system 70 as described in detail in Figs. 3 A - 3E, the volume flow ratio between the gas phase (second volume flow V2) and the liquid phase (first volume flow VI) can be increased from 2.5 to 6.0, which allows wastewater with up to 20% higher C SB concentrations to be treated compared to other Fenton / air processes for a given volume of reactor 75. This results in a decisive advantage of this process, since due to the high oxygen utilization rate, the consumption of peroxide (third volume flow V3) is reduced by 60 to 70% compared to alternative processes, thus reducing operating costs in the same range.

[0068] In contrast to existing oxidation technologies, the reactor 75 can be operated as a flow tube reactor due to the flow-through component 10 and the nozzle device 80, since the reaction takes place primarily in the flow-through component 10, whereby the reactor 75 only serves as a storage tank.

[0069] Reactor 75 is operated at 1 to 10 bar, preferably 2 to 6 bar. The reaction temperatures range between 60 and 150 °C, preferably 80 to 120 °C, with the operating temperature also depending on the oxidizability of the wastewater constituents. -13-

[0070] To achieve a microsuspension and increase mass transfer between the gas and liquid phases, additional surfactants such as polypropylene / polyethylene oxide copolymers can be used in reactor 75, which also have a foam-suppressing effect. The HLB (hydrophilic-lipophilic balance) range of the surfactants used is between 5 and 15, preferably between 8 and 12.

[0071] With System 70, the entire spectrum of organic compounds (aliphatic, aromatic, heterocyclic, oligomeric and polymeric, particulate and dissolved) can be oxidized to biocompatibility. Furthermore, wastewater from low to high COD concentrations can be reduced to a desired concentration (preferably 60-80%) in continuous operation without reactor conversion. System 70 can be used across all industries, for example, pharmaceuticals, chemicals, textiles, paper, electroplating, leachate and / or oil production wastewater, etc. Reactor 75 can also be used for processes other than those described above.

[0072] Fig. 2 shows a system 70 for treating a fluid according to a second aspect. The system 70 according to the second aspect largely corresponds to the system 70 according to the first aspect, and only the differences from the system 70 according to the first aspect are described.

[0073] The separation device 110 of the system 70 according to the second aspect differs from the separation device 110 of the system 70 according to the first aspect, but serves the same purpose. The separation device 110 comprises a float 104, in particular a flexible float 104, for separating the oil phase, as well as a suction pump 106 for suctioning or removing the oil phase from the reactor 75. A line from the float 104 to the suction pump 106 is designed as an internal discharge in the reactor 75.

[0074] The separated and separated oil phase can either be removed from the system 70 and disposed of permanently, for example, in hazardous waste landfills or by incineration. This can be particularly useful for separated non-oxidizable oils such as perfluorinated hydrocarbons. Alternatively, the separated and separated oil phase can be fed back into the reactor 75, as can be useful for separated oxidizable oils, for example. The refeed can -14- for example by means of the suction pump 106 via the circulation line and the nozzle device 80.

[0075] Fig. 3A shows a perspective view of the flow-through component 10 according to a first aspect. The flow-through component 10 comprises a tubular base body 20 of length L with a circular cross-section. The length L of the base body 20 is also the length of the flow-through component 10. The base body 20 can also have a different cross-section, such as a triangular, square, or oval cross-section. The shape of the base body 20 is described in more detail in Fig. 5.

[0076] The base body 20 has an inlet 60 on one side and an outlet 65 on an opposite side. A fluid can flow through the base body 20 in a flow direction RI, with the fluid flowing into the base body 20 at the inlet 60 and exiting again at the outlet 65. The base body 20 can also have multiple inlets and / or multiple outlets.

[0077] The flow-through component 10 further comprises a mounting structure 24. The mounting structure 24 is connected to the base body 20, but can alternatively be formed integrally with the base body 20. The mounting structure 24 is arranged at one end of the base body 20, but can also be arranged at a different location on the base body 20, depending on the respective conditions at the installation site. The mounting structure serves to attach or mount the mixing structure 10, for example, to the reactor 75.

[0078] The base body 20 has an inner surface 22 on which a mixing structure 30 is arranged. The mixing structure 30 is formed integrally with the base body 20. In other words, the mixing structure 30 can be described as a structured inner surface 22 of the base body 20. The mixing structure 30 can alternatively be formed as a separate component and arranged on the inner surface of the base body 20.

[0079] The mixing structure 30 comprises a plurality of separate structural elements 40, wherein the number of structural elements 40 can be varied and is preferably at least two. The structural elements 40 are designed as elevations that rise from the inner surface 22 toward a central axis of the base body 20. Alternatively, the structural elements 40 can also be designed as depressions that extend in an opposite direction. -15-

[0080] The structural elements 40 are distributed across the inner surface 22, with adjacent structural elements 40 directly adjacent to one another. Alternatively, the structural elements 40 can also be spaced apart from one another. A plurality of structural elements 40 are arranged in an inner circumferential direction R2, which extends along an inner circumference of the base body 20. Likewise, a plurality of structural elements 40 are arranged in the flow direction RI. A detailed description of the arrangement of the structural elements 40 can be found in the description of Fig. 3C. The shape of the structural elements 40 is described in more detail in Fig. 4.

[0081] The base body 20, the mounting structure 24, and the mixing structure 30 are made of sintered material or acid- and chemical-resistant stainless steel, preferably of technical ceramic material. The base body 20, the mounting structure 24, and the mixing structure 30 can alternatively be made of other materials that meet the requirements imposed by the wastewater to be treated and the reaction conditions in the reactor 75. The base body 20, the mounting structure 24, and the mixing structure 30 can be made of the same material or of different materials.

[0082] The flow-through component 10 is designed as a heterogeneous catalyst. For this purpose, the mixing structure 30 is doped or impregnated with a catalyst compound 50, such as a transition metal oxide or a combination of several transition metal oxides with atomic numbers 21 to 30, 39 to 48, 57 to 80, and 89 to 112. The catalyst compound 50 can also be incorporated into or applied to the mixing structure 30 by other manufacturing processes. Several different catalyst compounds 50 can also be used. When used in the acidic pH range, iron compounds are preferably used as the catalyst compound 50, and in the alkaline pH range, manganese compounds are used. The reactor 75 equipped with the flow-through component 10 can thus also be operated with heterogeneous catalysis.

[0083] Fig. 3B shows a sectional view of the flow-through component 10 according to the first aspect. The sectional plane is oriented such that the center axis of the base body 20 lies in the sectional plane. The structural elements 40 of the mixing structure 30 are arranged irregularly. Several structural elements 40 are arranged in the flow direction RI. The mixing structure 30 does not extend over the entire length L of the flow-through component 10, but can also extend over the entire length L. The -16- Flow component 10 has an average inner diameter DI. This is calculated from the internal volume of flow component 10 and the length L of flow component 10. The number of structural elements 40, the pitch, in particular the pitch angle, of the structural elements 40, and the height H of the structural elements 40 determine the shape of the resulting structural elements 40.

[0084] The average inner diameter DI is in a range of 5% to 20% of the reactor diameter DR of the reactor 75 in which the flow-through component 10 is used. The average inner diameter DI is preferably 15% of the reactor diameter DR. The length L of the flow-through component 10 is in a range of 5 times to 15 times the average inner diameter DI. The length L is preferably 12 times the average inner diameter DI.

[0085] Fig. 3C shows a perspective view of the negative mold of a mixing structure 30 of the flow-through component 10 according to the first aspect. The negative mold is used as a mold in the manufacture of the flow-through component 10 and serves to illustrate the arrangement of the structural elements 40.

[0086] The structural elements 40 are arranged, viewed in the direction of flow RI, in left-handed spirals or spiral forms SL and right-handed spirals or spiral forms SR. Individual structural elements 40 are components of more than one left-handed spiral form SL and more than one right-handed spiral form SR. The winding ratios of the left-handed spiral forms SL and the right-handed spiral forms SR correspond to Fibonacci numbers.

[0087] The number of left-handed spiral forms SL and right-handed spiral forms SR, their pitch angle, and the height H of the structural elements 40 determine the shape of the resulting structural elements 40. In the example shown, the structural elements 40 have a pyramidal shape. The preferred arrangement of the structural elements 40 shown is characterized by a quotient, which is defined by the height H of the structural elements divided by the average inner diameter DI and lies in the range from 0.05 to 0.5, preferably from 0.1 to 0.25.

[0088] The described design of the mixing structure 30 through the design and arrangement of the structural elements 40 enables a particularly advantageous mixing of the volume flows VI to V4 entering the flow component 10 at the inlet 60. The structural elements 40 generate highly dynamic turbulences, which -17- lead to the pronounced cavitation effects. In particular, the spiral arrangement of the structural elements 40 generates a rotational movement of the flowing volume flows VI to V4 around the flow direction RI.

[0089] The structural elements 40 may alternatively be arranged according to a different pattern or randomly.

[0090] Fig. 3D shows another sectional view of the flow-through component 10 according to the first aspect. The sectional plane is perpendicular to the flow direction RI. Several structural elements 40 are arranged in the inner circumferential direction R2.

[0091] Fig. 3E shows a perspective sectional view of the flow-through component 10 according to the first aspect. The sectional plane is oriented such that the central axis of the base body 20 lies in the sectional plane. The sectional view shows the spiral arrangement of the pyramidal structural elements 40.

[0092] Figs. 4A-D show different shapes of structural elements 40 of the flow-through component 10. In addition to the described shape of the structural elements 40 according to the first aspect, the structural elements 40 can also have other shapes. The structural elements 40 can, for example, be tetrahedral (Fig. 4A), parabolic (Fig. 4B), conical (Fig. 4C), pyramidal (Fig. 4D), or spherical segment-like. These shapes can be both symmetrical and asymmetrical. The dimensions of the structural elements 40 can be identical throughout the entire mixing structure 30, but can also vary. Furthermore, structural elements 40 of different shapes can be combined in the mixing structure 30.

[0093] Figs. 5A-D show different shapes of the base body 20 of the flow component 10. In addition to the tubular or cylindrical shape of the base body 20 described in the first aspect (Fig. 5A), the base body 20 can also have other shapes. The base body 20 can, for example, be hyperbolic (Fig. 5B), conical (Fig. 5C), or even multi-shell, for example conical (Fig. 5D). The highly dynamic turbulence of the flowing volume flows VI to V4 generated within the flow component 10 can be further influenced by the choice of the shape of the base body 20.

[0094] The mixing structure 30 can extend over the entire inner surface 22 of the base body 20 or can be formed only partially on the inner surface 22.

[0095] Fig. 6A shows a top view of a nozzle device 80. The nozzle device 80 comprises a multi-component nozzle 86 with a plurality of openings 85, in the example shown a three-component nozzle for dispensing the first volume flow V1, the second volume flow V2, and the third volume flow V3. The nozzle device 80 can alternatively comprise a single-component nozzle, a two-component nozzle, or a multi-component nozzle for dispensing more than three volume flows.

[0096] The multi-component nozzle 86 is rotationally symmetrical, and the openings 85 are arranged in a uniform ring pattern. This results in a homogeneous composition of the total volume flow consisting of the three individual volume flows.

[0097] The use of single- or multi-component nozzles depends on the components of the wastewater or fluid to be treated, the pH range suitable for the oxidation of the components and the pH-dependent catalyst system.

[0098] Fig. 6B shows a sectional view of the nozzle device 80 designed as a three-component nozzle. The multi-component nozzle 86 comprises a feed, a chamber and at least one opening 85 for each volume flow to be supplied. The multi-component nozzle 86 comprises a feed and a chamber for the first volume flow VI, the second volume flow V2 and the third volume flow V3. Each of the volume flows VI, V2 and V3 passes through the respective feed into the respective chamber of the multi-component nozzle 86 and exits the multi-component nozzle 86 through the respective at least one opening 85. The multi-component nozzle 86 shown is a multi-component nozzle 86 with external mixing, so the volume flows VI, V2 and V3 only mix after exiting the openings 85 of the multi-component nozzle 86. Alternatively, a multi-component nozzle 86 with internal mixing can also be used, in which the volume flows are already mixed within the multi-component nozzle 86.

[0099] The first volume flow VI (wastewater propulsion jet) exits the center of the multi-component nozzle 86 and has a flow velocity of 15 to 30 m / s. The third volume flow V3 (peroxide) exits from annularly arranged openings 85, which are arranged adjacent to the first volume flow VI. The second volume flow V2 (air) exits from the outermost annularly arranged openings 85. The multi-component nozzle 86 shown, designed as a three-component nozzle, is preferably suitable for the use of organic catalyst systems with a quinoid / benzenoid structure. -19-

[0100] Fig. 7A shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a first example using the system 70 according to the invention. The first example describes a system 70 for treating wastewater from chemical synthesis with a C SB concentration of 6.5 gO2 / L. The structural elements 40 of the flow-through component 10 are designed as pyramidal protuberances arranged on different left-handed turns or spiral forms SL and right-handed turns or spiral forms SR. The turn ratio between left-handed spiral forms SL and right-handed spiral forms SR is 1.6 and corresponds to the Fibonacci number ratio of 8 to 5.

[0101] Reactor 75 is a 5.0-liter reactor and, in addition to standard internals, comprises the inventive combination of nozzle device 80 and flow-through component 10 with a cylindrical base body 20. The reactor is fed with 3.5 liters of wastewater from a chemical synthesis. The wastewater has a COD concentration of 6.1 gO2 / L. The pH is adjusted to 2.6, 1.5 mmol / L FeSO4*7 H2O is added, and the reaction solution is heated to 105 °C. After the pressure is adjusted to 3 bar and 105 °C is reached, the experiment begins with the addition of 15% hydrogen peroxide (third volume flow V3) at a dosing rate of 2.0 cm3 / min for a period of 40 minutes. The 100% mass of hydrogen peroxide added to oxidize the wastewater constituents corresponds to a redox equivalent of 0.35 (moles of peroxide per mole of COD) based on the COD value.

[0102] At the same time, an air flow (second volume flow V2) of 4.3 NL / min is supplied to reactor 75 for a period of 40 minutes via nozzle device 80 and flow-through component 10. The pH is kept constant at the specified pH of 2.6 using a control system. After a reaction time of 40 minutes, a COD reduction of 83% is determined. The 85% reduction is the result of the peroxide-induced COD reduction of 47.5% and the oxygen-induced COD reduction of 52.5%, which is attributable to the use of nozzle device 80 and flow-through component 10. The residues remaining after oxidation show a degree of biological degradation, characterized by a BOD5 / COD ratio of 0.76 (BOD5: Biological Oxygen Demand after five days), which ensures trouble-free biological degradation in a municipal wastewater treatment plant. -20-

[0103] Fig. 7B shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to the first example without the system 70 according to the invention. An analogous experiment with a system that, in contrast to the system 70 according to the invention, was equipped with only a two-component nozzle instead of the combination of nozzle device 80 and flow-through component 10, resulted in a COD conversion of only 61%, with 57.4% of the COD degradation occurring through peroxide and only 42.6% through atmospheric oxygen. A comparison of the two test results and the degradation rates shown in Figs. 7A and 7B demonstrates the improvement in the oxidative degradation of the wastewater constituents achieved by the present invention.

[0104] Fig. 8A shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a second example using the system 70 according to the invention. The second example describes a system 70 for the treatment of wastewater from the cosmetics industry with a COD concentration of 3.7 gO2 / L. The wastewater is a dispersion of unknown composition that arises during stirred tank cleaning. The biodegradability of the wastewater constituents is very poor, showing a BOD5 / COD ratio of only 0.32. A BOD5 / COD ratio of > 0.6 should be achieved to ensure trouble-free operation of a biological wastewater treatment plant.

[0105] The base body 20 of the flow-through component 10 is hyperbolically shaped to maximize the mass transfer between the gas / liquid / solid phases or to convert them into a suspension. The structural elements 40 of the flow-through component 10 are designed as tetrahedral protrusions, whose height H is 25% of the average inner diameter DI of the flow-through component 10. The structural elements 40 are arranged on 13 left-handed turns or spiral forms SL and 8 right-handed turns or spiral forms SR. The winding ratio between left-handed spiral forms SL and right-handed spiral forms SR thus corresponds to the Fibonacci number ratio of 13 to 8.

[0106] To achieve biocompatibility of the wastewater constituents, 3.5 liters of wastewater are adjusted to pH 2.8, mixed with 2.0 mmol / L ferrous sulfate, and heated to 110 °C. The reactor pressure is 3 bar. Subsequently, an 8.1% hydrogen peroxide solution (third volume flow V3) is added at a rate of 1.5 cm3 / min and air (second volume flow V2) at a rate of 2.8 NL / min over a period of 60 minutes using the nozzle device 80 and the flow-through component 10. -21-

[0107] In this case, a COD reduction of 66% was achieved, thus also meeting the required biocompatibility with a BOD5 / COD ratio of 0.68. The COD reduction achieved by peroxide in this example is 36.4%, and the oxygen-induced reduction is 63.6%. The high hydrodynamic turbulence and cavitation effects prevailing in the flow component 10 result in a high mass transfer between the forming phases. This is also linked to the high degree of conversion achieved.

[0108] Fig. 8B shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to the second example without the inventive system 70. An analogous experiment with a system that, in contrast to the inventive system 70, was equipped with only a two-fluid nozzle instead of the combination of nozzle device 80 and flow-through component 10, resulted in a conversion of only 38% due to the phase separation taking place in the reactor. The COD reduction caused by hydrogen peroxide was 68.7%, and that caused by the added atmospheric oxygen was only 32.3%.

[0109] The comparison of the two test results and the degradation rates shown in Fig. 8A and 8B shows the improvement in the oxidative degradation of the wastewater constituents achieved by the present invention.

[0110] Figure 9 shows a diagram of the kinetics of the oxidative degradation of wastewater constituents according to a third example using the system 70 according to the invention. The second example describes a system 70 for treating mixed wastewater consisting of wastewater from various industrial sectors, such as those generated by waste disposal companies. The mixed wastewater to be disposed of has a COD concentration of 7.3 gO2 / L. The wastewater constituents are not biodegradable. The BOD / COD ratio is only 0.24 and cannot be fed into a biological treatment plant.

[0111] The goal of wastewater treatment is to ensure the biodegradability of its constituents. A specific problem with this type of wastewater is the separation into an oil and water phase that occurs at higher temperatures. As a result, the oil phase floating in the reactor is no longer accessible to oxidation. The solution to this problem lies in the inventive separation and removal of the oil phase using the separation device 100 and its refeeding into the reactor.

[0112] The base body 20 of the flow-through component 10 is cylindrical. The system 70 also includes the separating device 100. The structural elements 40 of the The flow components 10 are tetrahedral in design and are arranged on 13 left-handed turns or spiral forms SL and 8 right-handed turns or spiral forms SR. The winding ratio between left-handed spiral forms SL and right-handed spiral forms SR thus corresponds to the Fibonacci number ratio of 13 to 8. The quotient of the height H of the structural elements and the average inner diameter DI of the flow components 10 is 0.12.

[0113] For the oxidative treatment of this wastewater, 3.5 liters of the wastewater are adjusted to a pH of 3.1, mixed with 4.0 mmol / L ferrous chloride, and heated to 110 °C. Irreversible phase separation occurs even during heating. The reactor pressure is 3 bar. After heating is complete, hydrogen peroxide is added (third volume flow V3) at 2.0 cm3 / min of a 16.8% solution for 55 minutes, and the resulting oil phase is extracted using the separation device 110. The separated oil phase is returned to the reactor 75 via the circulation line 115, the nozzle device 80, and the flow-through component 10. The oil / water flow returned to the reactor 75 from the separation device 110 is a maximum of 10% of the circulation flow, in this case 0.05 L / min.

[0114] During the 55-minute reaction, 5.5 NL / min of air (second volume flow V2) is fed into the reaction mixture via the nozzle device 80 and the flow-through component 10. The air / liquid volume flow ratio in the flow-through component 10 is 3.0 at 3 bar. Without the mixing component 10, at 3 bar pressure, only air / liquid volume flows < 2.0 lead to adequate mixing of the two phases and acceptable conversion values. In this case, with an air / liquid volume flow ratio of 3.0 and oil recirculation, a COD conversion of 62% was achieved, resulting in a BOD5 / COD ratio of 0.67.

[0115] The achieved COD conversion of 62% is attributable to the amount of peroxide used (46%) and the added atmospheric oxygen (54%). Complete mineralization takes place in a biological wastewater treatment plant.

[0116] Fig. 10 shows a flow diagram of a method 200 according to the invention for treating a fluid. The fluid may be organically contaminated wastewater that is to be oxidized by the method. However, the method can also be used to treat other types of fluid. -23-

[0117] In a step S200, a first volume flow VI and a second volume flow V2 are fed to a reactor 75 by means of a nozzle device 80 and a flow-through component 10. The first volume flow VI and the second volume flow V2 are mixed in a step S210 while flowing through the flow-through component 1. The mixing is promoted by a mixing structure 30 arranged within the flow-through component 10. In addition to the first volume flow VI and the second volume flow V2, further volume flows can also be fed and mixed.

[0118] A phase settling in reactor 75, such as an oil phase, is separated and removed in a step S220 by means of a separation device 110. The separated phase is returned to reactor 75 in a step S230 for further treatment.

[0119] Fig. 11 shows a flow diagram of a computer-implemented method 300 according to the invention for controlling the system 70 according to the invention. The computer-implemented method 300 can control the system 70 such that the process of treating a fluid can be dynamically adapted to changing parameters of the fluid introduced into the system 70 or the fluid discharged from the system 70.

[0120] Due to the changing constituents of the fluids or wastewater to be treated and the associated different disposal targets, standard control and regulation algorithms are insufficient to meet the required wastewater treatment targets and associated wastewater pollution limits. The computer-implemented method 300 according to the invention can operate the wastewater treatment process in the system 70 according to the invention dynamically within a previously defined multidimensional optimal range.

[0121] In a step S300, an actual value WZ1 of at least one target variable ZG is detected by means of a sensor S. The at least one target variable ZG is the COD concentration of the fluid supplied to the system 70 or of the fluid currently contained in the system 70. The at least one target variable ZG can alternatively be another technical parameter such as the AOX concentration or the color, or a commercial or business parameter such as the operating costs, or a combination of technical and commercial parameters. The sensor S is -24- configured to measure the C SB concentration. Sensor S can alternatively be configured to measure other technical or commercial parameters. The measurement of the actual value WZ1 by sensor S can be replaced by another method of determining the actual value WZ1, such as by taking a sample and determining the respective parameter by analyzing the sample.

[0122] In step S310, a control value WS2 of at least one control variable SG is determined using an optimization algorithm. The optimization algorithm determines the control value WS2 of the at least one control variable SG from the actual value WZ1 of the target variable ZG, a target value WZ2 of the target variable ZG, and an actual value WS1 of the control variable SG. The optimization algorithm can include additional parameters for determining the control value WS2.

[0123] The control variable SG is the pH value of the fluid or wastewater treated by the system 70, or a dosage value for the peroxide (third volume flow V3), air (second volume flow V2), or catalyst (fourth volume flow V4) supplied to the system 70 or the reactor 75 via the nozzle device 80 and the flow-through component 10. The control variable SG can also be other controllable parameters of the system 70, such as the temperature or the reactor inflow flow.

[0124] In a step S320, the control variable SG is set to the control value WS2 by means of a control device SV contained in the system 70. The control device SV can, for example, be a pump that conveys one of the second volume flow V2, the third volume flow V3, or the fourth volume flow V4 and can thus be controlled to meter the volume flows V2 to V4. The control device SV can also be another device for influencing control variables SG of the system 70, such as a control device for the wastewater feed flow and thus the hydrodynamic residence time or heating elements.

[0125] More than one target variable ZG can also be considered and more than one control variable SG can be influenced. In this case, the system 70 can comprise more than one sensor S and more than one control device SV. This results in a multidimensional optimization space in which an optimal combination of the control variables SG to be influenced is to be found.

[0126] The optimization algorithm is an evolutionary-strategic optimization algorithm. Evolutionary-strategic algorithms belong to the stochastic, metaheuristic optimization methods, and they are based on the evolution of natural organisms. Five groups of evolutionary-strategic algorithms are generally distinguished: genetic algorithms, evolutionary strategies, genetic programming, differential evolution, and evolutionary programming. The optimization algorithm in this context is an algorithm from the group of genetic algorithms.

[0127] The search for a solution (i.e. the control value WS2 of at least one control variable SG for which the target value WZ2 of the target variable ZG is achieved) or a solution space (combination of the control values ​​in the case of several control variables SG for which the target value WZ2 of the target variable ZG or the target values ​​in the case of several target variables ZG are achieved as best as possible) is modeled on the natural process of evolution that takes place in the environment. Darwin's theory of the evolution of species is taken into account. The starting point is a large number (population) of individuals, with each individual representing a potential solution to the problem. The problem to be solved is defined by an objective function. Each individual is assigned a so-called fitness, according to which each individual is evaluated. Fitness represents how well the respective individual fulfills the objective function.

[0128] Two operations, mutation, crossover, and selection, are applied to the individuals in the population. In mutation, the values ​​of individual control variables (SG) are randomly changed. In crossover, the values ​​of individual control variables (SG) of two individuals are exchanged. In selection, a new population of individuals is formed by selecting individuals from the existing population. The individuals with the best fitness values ​​are chosen.

[0129] For each population, individual individuals are modified through mutation and crossover, creating new individuals. A new population of individuals is then created through selection. Mutation and crossover are then applied to this new population, and yet another new population is created through selection. The algorithm repeats this process until a termination criterion is met. The termination criterion in this case is defined as the maximum number of populations to be created. The maximum number is 100 generations.

[0130] In the simplest case of the optimization algorithm presented here, with only one target variable (ZG) and only one control variable (SG), the objective function consists of the target variable (ZG). Individuals in the populations differ only in their values ​​of the control variable (SG).

[0131] The optimization algorithm can alternatively be another type of evolutionary strategic optimization algorithm, a gradient method optimization algorithm or another type of optimization algorithm. -27- REFERENCE SYMBOL 10 Flow component 20 base bodies 22 inner surface 24 Assembly structure 30 Mixed structure 40 structural element 50 catalyst compound 60 entrance 65 Outlet 70 systems 75 reactor 80 nozzle device 82 Feed 85 Opening 86 Multi-component nozzle 90 inner body 95 Circulation flow 100 Separator 102 Overhang up edge 104 floats 106 Suction pump 110 Circulation pump 115 Circulation line 120 Shower 130 exhaust air extraction 150 processor 200 procedures 300 Computer-implemented procedure DI Average inside diameter flow component DR reactor diameter -28- L length RI flow direction R2 inner circumferential direction S Sensor SG control variable SL Left-handed spiral shape SR Right-handed spiral shape SV control device V 1 First volume flow V2 Second volume flow V3 Third volume flow V4 Fourth volume flow V5 Fifth volume flow WS1 actual value WS2 tax value WZ1 actual value WZ2 target value ZG target value S200 Feed S210 Mixing S220 Separation S230 Return S240 Discharge S300 Capture S310 Determine S320 Setting

Claims

-29- Claims 1. A flow-through component (10) for mixing at least a first volume flow (VI) and a second volume flow (V2), the flow-through component (10) comprising: a base body (20) through which the first volume flow (VI) and the second volume flow (V2) flow in a flow direction (RI); and a mixing structure (30) arranged within the base body (20) with a plurality of structural elements (40), wherein the plurality of structural elements (40) are at least partially in fluidic contact with at least one of the first volume flow (VI) and the second volume flow (V2), and wherein at least two of the structural elements (40) are arranged along an inner circumferential direction (R2) of the base body (20).

2. Flow-through component (10) according to claim 1, wherein the shape of the structural elements (40) is determined by the number of structural elements (40), the pitch of the structural elements (40) and the height (H) of the structural elements 40.

3. Flow-through component (10) according to claim 1 or 2, wherein at least two of the structural elements (40) are arranged along the flow direction (RI).

4. Flow-through component (10) according to one of claims 1 to 3, wherein the structural elements (40) are arranged at least partially in a spiral shape along the flow direction (RI).

5. Flow-through component (10) according to claim 3, wherein the structural elements (40) are arranged along the flow direction (RI) at least partially in at least one of a left-handed spiral shape (SL) and a right-handed spiral shape (SR). -30- 6. Flow-through component (10) according to claim 5, wherein winding ratios of the left-handed spiral form (SL) and / or the right-handed spiral form (SR) correspond to Fibonacci numbers.

7. Flow-through component (10) according to one of the preceding claims, wherein the base body (20) has at least one or more of a cylindrical, conical, hyperbolic and double-conical shape along the flow direction (RI).

8. Flow-through component (10) according to one of the preceding claims, wherein at least one of the structural elements (40) has one of a tetrahedral, parabolic, conical and pyramidal shape.

9. Flow-through component (10) according to one of the preceding claims, wherein the mixing structure (30) at least partially comprises a catalyst compound (50).

10. A system (70) for treating a fluid, the system (70) comprising: a reactor (75); a flow-through component (10) according to one of claims 1 to 9 arranged on the reactor (75); and a nozzle device (80) configured to supply at least a first volume flow (V1) and a second volume flow (V2) into the flow-through component (10).

11. A system (70) for treating a fluid, the system (70) comprising: a reactor (75); a flow-through component (10) arranged on the reactor (75); and a nozzle device (80) configured to supply at least a first volume flow (V1) and a second volume flow (V2) into the flow-through component (10), wherein the nozzle device (80) comprises a multi-component nozzle with external mixing (86). -31- 12. System (70) according to claim 11, further comprising: a separation device (100) for separating a phase from the reactor (75), wherein the separation device (100) comprises at least one of a ring line, an overflow edge (102) or a float (104) and wherein the separation device (100) comprises a suction pump (106) for sucking out the phase and returning the phase by means of the nozzle device (80) into the flow-through component (10) and / or discharging the phase.

13. System (70) according to claim 11 or 12, further comprising: a control device (SV) configured to meter the amount of the respective volume flow (VI; V2) supplied to the reactor (75), wherein the control device (SV) sets a control variable (SG) to a control value (WS2), wherein the control value (WS2) is determined by means of an optimization algorithm.

14. System (70) according to one of claims 10 to 13, wherein the reactor (75) comprises an inner body (90) for generating a reactor-intrinsic recirculation flow, wherein the flow-through component (10) is arranged at least partially within the inner body (90).

15. System (70) according to one of claims 11 to 14, further comprising a sensor (S) which is arranged in the reactor (75) and is configured to detect an actual value (WZ1) of at least one target variable (ZG).

16. System (70) according to claim 15, further comprising a processor (150) configured to determine the control value (WS1) of the control variable (SG) from the actual value (WZ1) of the at least one target variable (ZG), a target value (WZ2) of the at least one target variable (ZG) and an actual value (WZ1) of the control variable (SG) by means of the optimization algorithm.

17. System according to one of claims 11 to 16, wherein the control variable (SG) is a pH value of the fluid treated by the system (70) or a dosage value for peroxide, air or catalyst supplied to the system (70) or the reactor (75) by means of the nozzle device (80) and the flow-through component (10). -32- 18. System according to one of claims 11 to 17, in which the target variable (ZG) is preferably the chemical oxygen demand (COD concentration), more preferably the color or more preferably the AOX concentration (adsorbable organic bound halogens) of the fluid supplied to the system (70) or of the fluid currently contained in the system (70), in particular the target variable (ZG) is a technical or a commercial parameter.

19. System according to one of claims 11 to 18, wherein the optimization algorithm is a gradient descent optimization algorithm or an evolutionary optimization algorithm, in particular the evolutionary optimization algorithm is a genetic algorithm.

20. System according to one of claims 11 to 19, in which the flow-through component (10) is arranged to be arranged interchangeably depending on the medium of the fluid in the reactor (75), in particular the flow-through component (10) is not fixedly connected to the nozzle device (80).

21. A system according to any one of claims 12 to 20 when dependent on claim 12, wherein the separation device (100) adaptively adjusts to the level of the supernatant phase to remove only the supernatant phase.

22. System according to one of claims 12 to 21, when dependent on claim 12, in which the suction pump (106) sucks the floating phase and returns the floating phase to the flow-through component (10) by means of the multi-component nozzle with external mixing (86).

23. A method (200) for treating a fluid in a reactor (70) having a flow-through component (10) according to any one of claims 1 to 9, the method comprising the steps: Feeding (S200) at least a first volume flow (VI) and a second volume flow (V2) into the flow-through component (10) by means of a nozzle device (80) designed as a multi-component nozzle with external mixing (86); and -33- Mixing (S210) the first volume flow (VI) and the second volume flow (V2) within the flow-through component (10) to promote a reaction chain between the first volume flow (VI) and the second volume flow (V2).

24. The method (200) according to claim 23, further comprising the step of separating (S220) a phase from the reactor (75) by means of a separation device (100).

25. The method (200) according to claim 23 or 24, further comprising the step of returning (S230) the separated phase by means of the nozzle device (80) into the flow-through component (10).

26. The method (200) according to any one of claims 23 to 25, further comprising the step of removing (S240) the deposited phase.

27. A computer-implemented method (300) for controlling a system (70) according to any one of claims 10 to 22 for treating a fluid in a reactor (75) having a flow-through component (10), the method comprising: Detecting (S300) an actual value (WZ1) of at least one target variable (ZG) of the system (70) by means of a sensor (S); Determining (S310) a control value (WS2) of at least one control variable (SG) from the actual value (WZ1) of the target variable (ZG), a target value (WZ2) of the target variable (ZG) and an actual value (WS1) of the control variable (SG) by means of an optimization algorithm; and Setting (S320) the control variable (SG) to the control value (WS2) by means of a control device (SV) contained in the system (70).

28. The computer-implemented method (300) of claim 27, wherein the optimization algorithm is a gradient descent optimization algorithm or an evolutionary strategic optimization algorithm. -34- 29. Computer-implemented method (300) according to claim 27 or 28, wherein the at least one target variable (ZG) is a technical or a commercial parameter.

30. Computer-implemented method (300) according to one of claims 27 to 29, wherein the at least one control variable (SG) is the pH value of the fluid treated by the system (70) or a dosage value for peroxide, air or catalyst supplied to the system (70).

31. Computer-implemented method (300) according to one of claims 27 to 30, wherein the target variable is preferably the chemical oxygen demand (COD concentration), preferably the color or preferably the AOX concentration (adsorbable organic bound halogens) of the fluid supplied to the system (70) or of the fluid currently contained in the system (70).

32. A computer program comprising instructions which, when executed by a computer, cause the computer to execute the computer-implemented method (300) according to any one of claims 27 to 31.

33. A computer-readable medium comprising instructions which, when executed by a computer, cause the computer to perform the computer-implemented method (300) of any one of claims 27 to 31.

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