Reactor, apparatus and method for synthesizing products by strong exothermic reactions

Abstract

A reactor for performing a synthesis process for producing a product from at least two reactants, the reactor comprising: a body having a longitudinal axis, an inflow side and an outflow side; an interior; at least two reactant conduits, each connected on the inflow side to at least one distributor channel; at least one product conduit connected on the outflow side to the at least one collection channel; at least one distribution section comprising at least two distributor channels and at least one diverter; at least one mixing section in which at least two distributor channels are connected via a mixing channel and at least two reactants can be combined; at least one reaction channel; at least one collection section comprising at least one collection channel; at least one inflow-side feed conduit for the entry of a heat transfer medium into the interior; the heat transfer medium can flow around at least a part of the length of the at least one reaction channel in the interior, and / or at least one heat exchange channel in which the heat transfer medium can flow is provided, wherein the at least one sub-section is arranged adjacent to the at least one reaction channel, and wherein the at least one heat exchange channel and the at least one reaction channel are separated from each other by a common channel wall, and wherein the at least one reaction channel is a multiple spiral comprising two or more spiral channels, each spiral channel of the multiple helixes is connected via at least one mixing section to at least one distributor channel of each of the at least two reactants, and wherein on the outflow side each spiral channel of the multiple helixes is connected to at least one collecting channel.

Description

[0001] This invention relates to reactors, and to methods for producing products in a strongly exothermic reaction of two or more reactants, and to a method for producing the reactor using computer-implemented processes and additive manufacturing processes.

[0002] Strongly exothermic reactions include, for example, alkoxylation reactions, in which a chain initiator (reactant 2) reacts catalyzed with at least one epoxide (reactant 1) to yield an alkoxylate. Suitable chain initiators include compounds having reactive hydrogen atoms (reactant 2), such as alcohols, fatty alcohols, phenols, alkylphenols, amines, carboxylic acids and their esters, thiols, and imidazolines.

[0003] The alkyl oxides used (reactant 1) particularly include ethylene oxide (EO) and propylene oxide (PO), as well as 1-epoxybutane (BO) and phenyl ethylene oxide (SO). Alkoxylation using ethylene oxide is also known as ethoxylation. Repeated ethoxylation of fatty alcohols yields fatty alcohol polyethylene glycol ethers, which have a very wide range of applications, including as surfactants and emulsifiers. Therefore, the ethoxylation of fatty alcohols is carried out industrially.

[0004] Industrially, alkoxylation is carried out in both batch and continuous processes. In a batch process, a limited batch of substrate, alkyl epoxide, and catalyst is first loaded into a reaction vessel and reacted. After the reaction is complete, the alkoxylated product is removed from the reaction vessel. The batch process mode is particularly suitable for small-scale production (specialty chemicals).

[0005] For larger volumes, a continuous operation mode is used, in which reactants are continuously introduced into the reactor, reacted therein, and products are continuously removed. This so-called continuous reactor employs a continuous flow process.

[0006] In the production methods of specialty chemicals using microreactor technology, reactants still react continuously, but with significantly lower mass flow rates, resulting in a smaller product yield compared to classic continuous processes. The advantages of microreactor technology include higher process strength, which leads to better controllability of the reaction, ensuring higher energy efficiency, and requiring less equipment installation space. In particular, compared to batch processes, microreactor technology allows for better heat removal because the same amount of substance reacts for a longer period in a smaller reaction space.

[0007] In contrast, batch processes involve reacting equal amounts of material in a large reaction space over a short period of time, requiring the heat of reaction to be removed over a long distance. This always carries the risk of hot spots within the batch reactor, which can promote the formation of undesirable byproducts. Microreactor technology, on the other hand, avoids hot spots through better thermal management, suppressing undesirable side reactions and ultimately resulting in better product quality.

[0008] The following literature provides an introduction to microreaction techniques:

[0009] Ehrfeld, W., Hessel, V., Löwe, H.: Microreactors: New Technology for Modern Chemistry, published online on April 29, 2004, Wiley‐VCH Verlag GmbH, DOI:10.1002 / 3527601953.

[0010] US 2006 / 045828A1 discloses a reactor with multiple reaction zones containing a catalyst for the catalytic conversion of a feed stream. This produces a product stream, wherein each reaction zone is formed by multiple coaxially arranged helical reaction tubes having a compact, coiled structure, and the reactor is proposed particularly for catalytic reactions of methane steam reforming. Multiple heat exchanger tubes connect the reaction tubes of different reaction zones, wherein these heat exchanger tubes are in a helical configuration.

[0011] EP2603543B1 discloses a microreaction process for the production of polyether alcohols. EP 3 603 795 A1 discloses a reactor for a continuous reaction of two reactants. This document suggests introducing a second reactant from a second channel through spaced-apart orifices into a reaction channel traversed by the first reactant and arranged in a self-supporting manner within the reactor, which may have a cooling medium flow around it to form the reaction mixture. The channel, and particularly the reaction channel, is simultaneously subjected to a cooling medium flow surrounding it. The disadvantages of this reactor and the associated reaction are severely limited throughput performance and difficulty, if not complete, control over the reaction in the reaction zone. The latter has an adverse effect on the product.

[0012] Therefore, the object of the present invention is to provide a reactor that substantially overcomes the disadvantages described and a corresponding manufacturing method.

[0013] This objective is achieved according to the invention by a reactor as described in claim 1 and an apparatus as described in claim 17, wherein the reactor is producible by a production method as described in claim 21. Furthermore, this objective is achieved according to the characteristics of claim 26 by a strongly exothermic synthesis reaction.

[0014] The reactor according to the invention is used for a method of synthesizing a product from at least two reactants, and includes:

[0015] - The main body, which has a longitudinal axis, an inflow side and an outflow side;

[0016] - Internal; at least two reactant conduits, each connected on the inflow side to at least one dispenser channel;

[0017] - At least one product conduit connected to at least one collection channel on the outflow side;

[0018] - At least one inflow-side allocation section, which includes

[0019] In at least one reactant conduit, particularly in all reactant conduits, there is at least one shunt and at least two (primary) distributor channels;

[0020] - At least one mixing section, wherein at least two dispenser channels are connected via a mixing channel and at least two reactants are combinable, particularly in downstream secondary dispenser channels;

[0021] - A reaction section, which includes at least one reaction channel, particularly two or more reaction channels;

[0022] - At least one collection section, which includes at least one collection channel;

[0023] - (at least) one inlet conduit for the heat transfer medium to enter the interior; and (at least) one outlet conduit for the heat transfer medium to leave the interior, wherein

[0024] - A heat transfer medium may flow around at least a portion of the length of at least one reaction channel within the interior and / or at least one heat exchange channel in which the heat transfer medium may flow is provided, wherein the at least one sub-section is arranged adjacent to at least one reaction channel, and wherein at least one heat exchange channel and at least one reaction channel are separated from each other by a common channel wall.

[0025] Here, at least one reaction channel is a multi-helix comprising two or more helical channels, wherein on the inflow side, each helical channel of the multi-helix is ​​connected via at least one mixing section to at least one dispenser channel of each of at least two reactants, and wherein on the outflow side, each helical channel of the multi-helix is ​​connected to at least one collection channel.

[0026] This reactor is particularly suitable for producing products via a strongly exothermic reaction in or between liquid reactants. Specifically, the reactor is configured to employ liquid reactants that are gaseous under atmospheric conditions and, due to pressure, exist in a liquid phase in at least one reactant conduit or within the reactor.

[0027] The body is advantageously elongated and includes an interior. The term "interior" is not intended to be construed as restrictive, but rather describes the volume enclosed by the body. The interior may include solid material, cavities, channels, etc. The interior may also be divided or segmented into two or more sections.

[0028] A primary distributor channel should be understood to mean a channel in which reactants, reactant mixtures, or reactant streams are introduced for subsequent distribution into multiple downstream channels (especially mixing channels) arranged, for example, in the circumferential direction. The primary distributor channel is unreacted or substantially unreacted, particularly not for the main reaction used to produce the desired product.

[0029] A secondary distributor channel should be understood to mean a channel into which at least two reactants, reactant mixtures, and / or reaction streams from, for example, two primary distributor channels are introduced, such that the main reaction begins directly in the secondary distributor channel. Mixing sections typically form the transition from the primary distributor channel to the secondary distributor channel.

[0030] Reactant conduits and product conduits may be provided with known fixing components, such as flanges, threads, etc. In addition, the terms "on the inflow side", "on the outflow side", "inflow side", "outflow side", "top", "bottom", etc. should not be interpreted in a narrow sense, and refer to a rough arrangement, direction or orientation, so that they may also mean "close to".

[0031] The helical channels of a multi-spiral configuration ideally coil in the same direction and advantageously extend parallel to each other for most of their range. In other words, the helical channels of a multi-spiral configuration have the same or substantially the same angle of inclination. Taking into account the vertically aligned longitudinal axis of the reactor, the flow axis of the helical channels is advantageously inclined at 15° to 45° relative to the horizontal direction. The inclination of the flow axis is similarly derived for different arrangements of the longitudinal axis.

[0032] Depending on the outer radius of the multi-spiral configuration, it may contain 3 to 10 spiral channels, particularly 3 to 6 spiral channels. At the transition from the upstream distributor channel to the corresponding spiral channel, the spiral channel advantageously has an inlet cone that narrows in the flow direction. In an advantageous variant, this inlet cone comprises inlet sides with different widths and angles, wherein the lower inlet side in the main flow direction is gentler and aligned, for example, at least along the flow axis of the sub-section parallel to the corresponding spiral channel, and the upper inlet side is steeper and / or has a smaller radius.

[0033] In one embodiment of the reactor, it may be advantageous for the reactor to include two or more reaction channels in a multi-helix configuration, wherein the outer multi-helix of the outer reaction channel concentrically surrounds at least the inner multi-helix of the inner reaction channel, and wherein the inflow side of each reactant conduit is directly or indirectly connected to each multi-helix.

[0034] The connection between the multi-screw and the primary distributor channel is achieved, in particular, via the mixing section and the secondary distributor channel. Even though the secondary distributor channel and the collection channel are described and interpreted as separate from the multi-screw in this case, the multi-screw may also include a secondary distributor channel on the inflow side and / or similarly a collection channel on the outflow side.

[0035] In another embodiment of the reactor, it may be advantageous to configure each reaction channel of the multi-helix reactor, with the inflow side connected to a dedicated secondary distributor channel and / or mixing section, in the case of two or more reaction channels / multi-helices.

[0036] In another embodiment of the reactor, it may be advantageous that at least one additional secondary distributor channel and / or an inlet into each spiral channel is arranged downstream of at least one inflow-side secondary distributor channel in the direction of the longitudinal axis.

[0037] Prior to complete conversion, an additional secondary distributor channel merges with the helical channel of the reaction channel, and reactants (e.g., reactant 1 already introduced at the beginning) and / or catalyst can be introduced at defined volumetric flow rates. This makes it possible, for example, to achieve complete conversion through the subsequent introduction of reactant 1 in the event of incomplete conversion of reactant 2. Downstream of the additional secondary distributor channel, the altered reaction mixture is again transported in the helical channel.

[0038] In another embodiment of the reactor, it may be advantageous to connect the outflow side collection channel or the outflow side discharge chamber to the outlet throttle valve and / or the outlet nozzle and / or include the throttle valve and / or the nozzle.

[0039] This arrangement makes it possible to achieve pressure increase and pressure homogenization in the multi-spiral reaction channels within the reactor. When the outlet throttle valve or outlet nozzle is controllable, this allows for control of the outlet-side pressure.

[0040] It is advantageous for the collection channels to be arranged in a cascaded manner. This may include helical channels leading to each individual multi-spiral structure within a corresponding first collection channel. These first collection channels are connected to each other, for example, via annular or conical sections or additional collection channels. The end connection channels include conduit connections in the flow direction to the discharge chamber and / or to the product conduit.

[0041] In another embodiment of the reactor, it is advantageous that the minimum width (B) of the cross-sectional area (A) of the helical channel is 0.8 mm to 3 mm, ideally 0.8 mm to 2 mm. The helical channel is advantageously sized such that laminar flow is formed within it. In the case of a circular cross-section, the diameter is advantageously 1.1 to 1.5 times the aforementioned width (B).

[0042] In principle, the cross-section / cross section of the helical channel can have any geometry, with particularly advantageous shapes for heat exchange including stretched groove shapes such as oval, elliptical, or rectangular cross sections. “Rectangular” should be understood to also include shapes that are substantially rectangular and in which, for example, the corners are rounded or the short side is a single arc, or other shapes such as parallelograms or trapezoids.

[0043] Here, the shortest path from each molecule to the first heat exchange wall should be half of the value mentioned above.

[0044] Advantageously, the flow cross-section of the helical channels in the reaction channel is fixed in size, so that the flow rate of the reaction mixture is the same or substantially the same in all helical channels of all reaction channels. In this way, the average residence time of the substance / individual molecule in the reaction section of the reactor is the same or substantially the same, so that all reaction sections in the reactor provide products with the same or at least very comparable quality.

[0045] In another embodiment of the reactor, it may be advantageous for the cross section (A) in the helical channel to have an elliptical, oval, or at least approximately rectangular basic structure, wherein the ratio of the minimum extent (width B) to the maximum extent (height H) of the cross section is advantageously not less than 0.5, ideally in the range of 0.2 to 0.06.

[0046] Ideally, in a vertical section, the maximum longitudinal extent of the transverse region A is aligned parallel to the longitudinal axis (height H), and the minimum longitudinal extent (width B) is oriented in the radial direction.

[0047] In other words, the spiral channel of the reaction channel takes the form of a gently sloping channel, which is spirally arranged at fixed intervals around the central longitudinal axis, wherein its long sides are aligned and aligned with each other in the direction of the longitudinal axis, such that the spiral channel spans a theoretical (envelope) cylindrical ring or annular groove. The long sides of the spiral channel are arranged parallel to or substantially parallel to the sides of the aforementioned theoretical annular groove.

[0048] In another embodiment of the reactor, it is advantageous to provide at least one sensor holder for housing and / or fixing the sensor, wherein the sensor holder includes a sensor pier connected at one end to a helical channel inside the reactor body, and wherein the sensor pier passes through the interior and through the reactor wall of the main body. Outside the main body, the sensor housed and fixed in this manner can be connected to a data receiver and / or control unit in a data conduction manner. The connection between the sensor pier and the channel inside the reactor forms a wall, particularly the channel wall, which serves as the measurement point for the free measuring end of the sensor.

[0049] The sensor holder and, in particular, the sensor base, are advantageously made of the same primary material as the reactor. The term "sensor base" should not be interpreted in a limiting sense, but rather refers to the enclosed conduit for a primary removable and replaceable sensor (e.g., a rod-shaped temperature sensor, vibration sensor, or flow sensor). The sensor base passes through the reactor interior at an angle and traverses wall sections and internal channels made of solid material until it reaches the measurement point. Therefore, the sensor base may include or be formed of: tubular or shell-like sections for traversing the internal cavity and open sections for penetrating the wall sections.

[0050] In another embodiment of the reactor, it is advantageous that each reaction channel, or at least one helical channel of each reaction channel, has a sensor base leading to its sensor holder, specifically multiple sensor bases arranged in the direction of the longitudinal axis. The advantage of this arrangement is that it allows for optimal detection of the reaction progress in the flow direction and influence of the reaction progress through open-loop and closed-loop control.

[0051] In another embodiment of the reactor, it is advantageous that each individual helical channel has at least one sensor base leading to it, and in particular, each reaction channel helical channel has at least two sensor bases leading to it. Preferably, each helical channel is connected to at least two sensor bases and a sensor holder via a corresponding measurement point.

[0052] Overall, it is also necessary to operate the reactor as energy-efficiently as possible. In another embodiment of the reactor, it is advantageous to include at least two separate heat exchange spaces or channels (HES) and / or groups of heat exchange channels internally, which are fluidly and spatially separated from each other by at least one internal separating element and / or section, wherein each HES / channel has at least one feed conduit and one discharge conduit, and wherein each HES / channel can utilize a different heat transfer medium and / or operate at its own temperature level.

[0053] The significant advantages of such dual-temperature operation are improved heat exchange and lower energy consumption. The first strongly exothermic reaction section can be operated, for example, via the first of two HES / channels at a higher volumetric flow rate and / or at a lower temperature level, particularly on the inflow side. Subsequent reaction sections (if exothermic, then only very slightly so) can be operated using the second HES / channel at a lower volumetric flow rate, a higher temperature level, and / or using a more economical heat transfer medium. Such a design and operating mode with at least two separate heat exchange loops is more economical and sustainable in the long run.

[0054] This alternative embodiment of the reactor can be advantageously improved by the following: the partition element includes an insulating layer and / or is at least partially made of insulating material.

[0055] The insulating layer may be, for example, an internal insulating layer and / or may be at least partially formed of, for example, metal foam, fibrous material or equivalent material or mixture of materials.

[0056] All apparatus used for conducting strongly exothermic reactions or for transporting or conveying explosive substances therein should advantageously have redundant risk protection. Particularly advantageous in other embodiments of the reactor is the presence of a protective shell surrounding it. This protective shell can be configured, in particular, to be blast-resistant, shatter-resistant, and / or fire-resistant, especially according to DIN EN1127-x.

[0057] This additional embodiment of the reactor with a protective shell can be advantageously improved by the following: the protective shell includes an extraction, filtration unit and / or an absorption unit and / or can be connected to the extraction, filtration unit and / or absorption unit.

[0058] The filtration or absorption unit particularly includes a non-flammable filter or absorption medium, which is made of, for example, zeolite, bentonite, metal foam or equivalent materials.

[0059] In another embodiment of the reactor, it may be advantageous to merge at least one spiral channel of the first reaction channel with at least one spiral channel of another reaction channel in the direction of the longitudinal axis downstream of at least one inflow-side distributor channel, in particular each of the spiral channels of the first reaction channel is merged with a corresponding different spiral channel of the other reaction channel.

[0060] In other words, two multiple helices become a single multiple helical structure. This design offers the following advantages: only the reaction section with low exothermic reaction characteristics benefits from a simplified construction, and therefore the reactor is easier to manufacture. Furthermore, by extending the reaction section within the helical channel, especially with the accompanying heat exchange channel, the overall reactor design remains compact and small.

[0061] Advantageously, the corresponding helical channels from each reaction channel / from each multi-helix are combined and continued downstream as / as a single (secondary) helical channel.

[0062] Improved mixing also improves reactant consumption and product quality. Based on the total reaction duration / molecular residence time in the reaction segment, the reaction segment in the secondary multiple helix corresponds to at least 50% of the total reaction duration, and particularly at least 75% of the total reaction duration.

[0063] In another embodiment of the reactor, it may be advantageous to have a spiral channel of at least two reaction channels downstream of at least one inflow-side distributor channel in the longitudinal direction into a common reaction tube via a collection unit, particularly a common reaction tube sized such that the residence time of the reaction mixture is such that...

[0064] - Corresponding to at least 50% of the total reaction duration, specifically

[0065] - Corresponding to at least 75% of the total reaction duration.

[0066] Unlike the reactor design described above, which features secondary multiple helices as secondary multiple helices / secondary reaction sections, this reactor tube is, in particular, a substantially straight tube.

[0067] In this case, the reaction mixture should be understood as a mixture of reactants, intermediates and / or products, the composition and concentration of each mixture portion of which vary in the flow direction (F) due to the ongoing reaction.

[0068] The collection unit indicating the transition from the reactor to the reaction tube can be the same as the collection channel described above. Therefore, the reactor is shorter in the longitudinal direction and thus easier and more economical to manufacture. The shared reaction tube is advantageously connected to a heat exchange loop and appropriately temperature-controlled, wherein this heat exchange loop can be independent of the reactor's heat exchange loop and / or structurally separate.

[0069] In another embodiment of the reactor, two reactors may be arranged in series. In particular, the collection section of the first reactor in the flow direction constitutes the distributor section of the second reactor and / or the discharge section of the first reactor forms the inlet section of the second subsequent reactor.

[0070] Such an arrangement is advantageous, for example, in chain synthesis where each step involves a high-energy reaction, such as the oxidation of ethylene to acetaldehyde in the first step and the first reactor, and the oxidation of acetaldehyde to acetic acid in a second step. Additional reactants and / or catalysts can be supplied upstream of the second reactor.

[0071] The invention further includes apparatus for a synthetic method of producing a product from at least two reactants using at least one reactor, wherein the at least one reactor is configured according to one of the variations and / or embodiments described above.

[0072] Further improved embodiments include at least two reactors configured and arranged in parallel according to any variants and / or embodiments described herein.

[0073] At least two parallel reactors may be connected to a common product conduit on the effluent side. Similarly, at least two parallel reactors may be connected to a common reactant conduit on the influent side.

[0074] In one embodiment of the apparatus, it is advantageous for at least two reactors to be connected on the outflow side to at least one common reaction tube, particularly to a common reaction tube sized such that the residence time of the reaction mixture in the reaction tube is such that...

[0075] - Corresponding to at least 50% of the total reaction duration, specifically

[0076] - Corresponding to at least 75% of the total reaction duration.

[0077] The reaction tube can also be a tubular reactor, or the reaction tube may be referred to as a tubular reactor. A common reaction tube is advantageously connected to a heat exchanger circuit, particularly via a dedicated heat exchanger circuit and / or a heat exchanger for temperature control. In another advantageous embodiment of the reaction tube, the reaction tube includes at least one elongated heat exchange element at its central location, which extends a portion of its length in the direction of the longitudinal axis of the reaction tube, such that the reaction space within the reaction tube has the shape of an annular groove or annular channel. In addition to the internal heat exchange element, the reaction tube may have a jacketed heat exchange element.

[0078] Similar to the reactor described above, the reaction tube may include at least one sensor holder for sensors, particularly for two or more sensors arranged in the longitudinal direction.

[0079] In another embodiment of the apparatus, it may be advantageous to connect a product conduit downstream of at least one reactor to a degassing unit comprising: a product conduit serving as a feed conduit, a first discharge conduit for the product and / or a mixture of substances containing the product, and a further gas discharge conduit for volatile substances, wherein the degassing unit is configured such that the pressure (p2) in the degassing unit is no greater than 2 bar, preferably no greater than 1 bar, and especially a vacuum of up to 0.5 bar.

[0080] At least one additional separation unit for separating substances from the product and / or purifying the product may be advantageously located downstream of the degassing unit.

[0081] The invention further includes a method for producing a reactor for synthesizing a product, wherein the reactor is configured according to any variation or embodiment described herein and wherein the reactor is manufactured by:

[0082] - Computer-implemented process (CIP) or part of the process, and

[0083] - Additive manufacturing process (AMP) via additive manufacturing apparatus (AMA).

[0084] CIP advantageously includes the following steps:

[0085] - Master data is provided from a database and / or via an input unit (HMI) for the process simulation program (CSD), wherein the master data may in particular be process data, flow data, material and medium data, and reaction data;

[0086] - Use a process simulation program (CSD) to simulate reactions in one step or in multiple steps;

[0087] - Generate design data via a process simulation program (CSD);

[0088] - Provide and receive executable control data for implementing AMA design data, wherein the executable control data is generated at least in part in the process simulation program (CSD) and / or the processor of AMP or AMA, and

[0089] -Execute AMP.

[0090] In this case, "providing" data should always be understood to mean that the data is at least temporarily stored on a non-volatile storage medium and retrieved by a corresponding device / accompanying processor unit and executed using a suitable (software) program in subsequent processing steps. The term "storage medium" should not be interpreted in a limiting sense, but includes internal and external storage media and all types of wired or wireless storage media. Furthermore, "providing" should also be understood to mean that, in a particular case, the unit described acquires the provided data or data packet and uses the data or data packet as intended by running an executable software program using at least one processor.

[0091] In another embodiment of the production method, AMP may be specified as a powder bed fusion process and / or a process with directional energy deposition, particularly a powder bed fusion process based on laser, electron beam, or plasma-induced deposition. Alternatively or additionally, AMA may be specified as being configured to perform this AMP. AMP may also be referred to as metal 3D printing and / or denote such 3D printing.

[0092] In another embodiment of the production method, it may be advantageous when the computer-implemented process or part of the process includes the following steps:

[0093] a) Provide process data and design parameters for CAD software.

[0094] b) Determine design data using CAD software or CAD models.

[0095] c) Provide control data for additive manufacturing equipment.

[0096] d) Production reactor via AMA.

[0097] Process data, especially material data and reaction technology and thermodynamic data, as well as dependencies. Step b) may also include single-step or multi-step simulations after repeating step a). Determining design data and / or CAD models is advantageously done through at least one strength determination, particularly via calculations and / or simulations based on the FEM (Finite Element Method).

[0098] The synthesis of the reaction is advantageously simulated, optionally multiple times, using simulation software such as CFD (Computational Fluid Dynamics). This simulation data (which may include process data, reaction data, thermodynamic data, and other data) is then provided, at least in part, to CAD software for reactor design and evaluation / adoption. This specifically involves creating a CAD model of the reactor as a dataset. The CAD model or dataset is provided to a display and / or output unit (e.g., a monitor) in at least one known display and / or output format, such as a .t_x file on a storage medium and / or output unit. Furthermore, it is advantageous for the CAD software to provide the number, type, and / or measurement locations of sensors / accompanying sensor holders as data and / or for the CAD model to include the number, type, and / or measurement locations of sensors. Ideally, the obtained CAD model can be used by a control unit with computational software or retrieved from a data storage device via computational software, wherein the computational software is configured to generate computational steps to verify the reactor's strength according to the corresponding CAD model using FEM (Finite Element Method). Advantageously, the steps of CFD simulation, CAD modeling, and / or FEM calculation are repeated iteratively once or multiple times until the required and / or legally mandated design (CAD model) is achieved, particularly the required reactor strength. In this case, the term "CAD model" as a dataset should not be interpreted in a restrictive sense, but rather includes not only the complete CAD model, but also all datasets, reports, and any data formats that are at least partially derived from and / or determined based on the CAD model using CAD software.

[0099] The invention also includes a storage medium comprising at least one executable program code.

[0100] - For carrying out at least one of the production methods according to the variations and implementation schemes mentioned herein, and / or

[0101] - Used to control the AMA, which is used to perform at least one of the production methods described herein in the variants and implementations.

[0102] The storage medium may be a portable, non-volatile storage device, such as a CD, DVD, or USB flash drive, or it may be part of a computer or processing unit (such as a computer, server, processor unit, or microprocessor unit). Furthermore, the associated data connections and / or interfaces are unrestricted and can be connected via wired or wireless means.

[0103] In one implementation, it may be advantageous for the storage medium to be integrated into the AMA or to be connected to or be able to connect to the AMA via data transfer.

[0104] The advantages and aspects of the reactors described herein apply in the same or similar manner to the equipment, and vice versa. The advantages and aspects of the production or synthesis methods described herein should also apply to the reactors and / or equipment, unless specific or limiting details are specified.

[0105] The present invention further includes a method for synthesizing a product by a (chemical) reaction, the method comprising the following steps:

[0106] a) Provide at least one reactor;

[0107] b) Provide the first liquid reactant;

[0108] c) Provide a second liquid reactant, wherein the second reactant may be a substrate containing or containing a catalyst;

[0109] d) Provide a liquid heat transfer medium;

[0110] e) Continuously supply the first reactant, the second reactant, and the heat transfer medium to the reactor;

[0111] f) The first liquid reactant and the second liquid reactant are continuously mixed in the mixing section of the reactor to obtain a liquid reaction mixture;

[0112] g) Downstream of the mixing section and inside the reactor, continuous conversion is carried out by reactant 1 with reactant 2, and in particular with the reaction products, to provide liquid products or product mixtures, and wherein, by means of the reactor, at least a portion of the heat of reaction generated during the reaction is transferred from the reaction mixture and / or product mixture to the heat transfer medium.

[0113] h) Continuously remove the product mixture from the reactor;

[0114] i) Continuously remove the heat transfer medium from the reactor;

[0115] The reactor is configured according to one of the variants and / or embodiments described herein, and / or the method utilizes or is carried out in an apparatus according to one of the variants and embodiments described herein.

[0116] Advantageously, the flow of the heat transfer medium is started before the first reactant, the second reactant and the heat transfer medium are continuously supplied to the reactor according to step e), and then the second reactant or both reactants are supplied to the reactor first.

[0117] In this case, the terms “conversion,” “synthesis (method),” or “(chemical) reaction” are used essentially synonymously in the absence of any specific indication. Furthermore, the term “reaction” should generally be understood to mean a chemical reaction that produces the desired (main) product. Reactants are especially pressurized liquefied substances that are gaseous or vaporous under atmospheric conditions.

[0118] In one variant of the synthesis method, it may be advantageous to provide a third reactant (reactant 3) comprising at least one catalyst or being a catalyst itself prior to step e), wherein the reactants are mixed continuously, simultaneously, or substantially simultaneously in step f). In this case, the reactor includes a corresponding third reactant conduit and, in particular, distributor channels, splitters, etc., similar to those described for the first reactant and / or the second reactant and its associated reactant conduit.

[0119] In one variant of the synthetic method, it may be further advantageous that the (process) pressure (p1) of the reactants is in the range of 10 bar to 100 bar, advantageously in the range of 20 bar to 80 bar, and ideally in the range of 35 bar to 65 bar.

[0120] In a variant of the synthesis method, it may be further advantageous that the method comprises a strongly exothermic reaction, particularly in which each mole of reactant 1 releases not less than 70 kJ, preferably not less than 80 kJ, and especially 85 kJ to 150 kJ per mole of reactant 1.

[0121] In a variant of the synthetic method, it may be further advantageous that the reaction in the reactor does not form volatile byproducts, particularly those requiring continuous removal (especially continuous distillation). The reaction, in particular, does not involve the continuous removal and discharge of byproducts, for example, in the vapor phase, to sustain the reaction.

[0122] In a variant of the synthetic method, it may be further advantageous to select the reaction from the group consisting of:

[0123] a. (polymer) addition,

[0124] b. Polymerization of monomers containing carbon double bonds (C=C double bonds)

[0125] c. Oxidation of organic compounds

[0126] d. Beckmann rearrangement for the synthesis of carboxylamides

[0127] e. Polymerization of butadiene and production of polybutadiene.

[0128] f.

[0129] In one variant of the synthesis method, a further advantage is that

[0130] - (poly)addition is alkoxylation, and

[0131] - The polymerization of monomers having carbon double bonds (C=C double bonds) is particularly free radical polymerization selected from the group consisting of acrylates, methacrylates, styrene, maleic anhydride and vinyl compounds.

[0132] In a variant of the synthetic method, it may be further advantageous that the reaction is an alkoxylation reaction for the production of alkoxylates, wherein:

[0133] a) The first liquid reactant is an epoxide selected from the group consisting of: ethylene oxide (EO), propylene oxide (PO), 1-epoxide butane (BO), and phenyl ethylene oxide (SO);

[0134] b) The second liquid reactant is a substrate / compound selected from the group consisting of alcohols, fatty alcohols, phenols, alkylphenols, amines, carboxylic acids and their esters, thiols and imidazolines.

[0135] In a variant of the synthesis method, it may be further advantageous to use a polymetallic cyanide complex catalyst, or an alkali metal or alkaline earth metal hydroxide (especially sodium hydroxide, potassium hydroxide and cesium hydroxide), or a basic catalyst (e.g. alkali metal alkoxides, especially sodium methoxide and potassium methoxide), or a tertiary amine.

[0136] In other variations of the synthesis method, the method can be configured as follows:

[0137] a. (Poly)addition is selected from the group of reactions:

[0138] - Alkoxylation, from HCN and ethylene oxide to produce 3-hydroxypropionitrile,

[0139] - (Meth)acrylates are prepared by reacting (meth)acrylic acid with alcohols or amines.

[0140] - Polyurethane is made from isocyanates and alcohols or amines.

[0141] - Addition reactions of carboxylic acids or carboxylic esters onto epoxides, such as the addition of bisphenol glycidyl ether, wherein the addition is achieved on bisphenol glycidyl ether.

[0142] - Hydrogenation reaction,

[0143] - Hydrosilylation,

[0144] - Hydroformylation;

[0145] b. Polymerization of monomers having carbon double bonds (C=C double bonds), such as, in particular, free radical polymerization, wherein the polymerization is selected from the group consisting of: polymerization of acrylates, methacrylates, styrene and vinyl compounds, polymerization of butadiene and production of polybutadiene;

[0146] c. Oxidation is selected from the group of reactions below:

[0147] - For example, using oxygen or peroxides, especially hydrogen peroxide, according to the HPPO method to epoxidize olefins, or also

[0148] - Oxidize isobutane to tert-butyl hydroperoxide.

[0149] - Oxidize methanol to formaldehyde.

[0150] - Oxidize propylene to acrolein.

[0151] - Oxidize acrolein to acrylic acid.

[0152] - Oxidize ethylene to acetaldehyde.

[0153] - Oxidize acetaldehyde to acetic acid.

[0154] - Directly oxidize ethylene to acetic acid.

[0155] - Oxidize cyclohexane to adipic acid.

[0156] Reactions that should also be understood in an oxidizing context, such as

[0157] - Nitrification

[0158] - Halogenation, wherein halogenation may be, for example, chlorination or chlorosulfonation.

[0159] In a variant of the synthetic method, a further advantageous oxidation reaction is Baeyer–Villiger oxidation. This involves using peracids such as peroxybenzoic acid, 3-chloroperoxybenzoic acid (MCPBA), peracetic acid, or trifluoroperacetic acid to oxidize the ketone to a carboxylic acid ester.

[0160] In a variant of the synthetic method, the oxidation reaction, which could be further advantageous, is the Andrussov method. This involves the ammoxidation of methane at 1000 °C over a Pt / Rh catalyst to produce hydrogen cyanide. CH4 + NH3 + 1.5 O2 → HCN + 3H2O. This is accompanied by an energy release of 474 kJ / mol.

[0161] The invention is illustrated in the accompanying drawings with the aid of exemplary embodiments, and the invention is described by way of example. In the accompanying drawings:

[0162] Figure 1 Two partial views (plan views) of the reactor in the first embodiment are shown.

[0163] Figure 2 It shows that according to Figure 1 A vertical cross-sectional view of the entire reactor.

[0164] Figure 3 The above section (allocation section) is shown in the form of an enlarged partial view according to... Figure 1 A cross-sectional view of the reactor.

[0165] Figure 4 A horizontal cross-sectional view of the reactor in the upper section is shown.

[0166] Figure 5 A horizontal cross-sectional view of the reactor at the height of the mixing section is shown.

[0167] Figure 6 The diagram is shown in the form of an enlarged partial view of the central section (reaction section) according to... Figure 1 A cross-sectional view of the reactor.

[0168] Figure 7 A horizontal cross-sectional view of the reactor at the height of the central section is shown.

[0169] Figure 8 The following section (collection section) is shown as an enlarged partial view based on... Figure 1 A cross-sectional view of the reactor.

[0170] Figure 9 A horizontal cross-sectional view of the reactor at the height of the lower section is shown, and

[0171] Figure 10A device with a reactor is shown in the second embodiment.

[0172] Figure 1 A partial view I of a reactor 100 in one embodiment is shown in a perspective side plan view. The reactor includes a body 102 that extends along a longitudinal axis 104 and has an inflow side 106 and an outflow side 108. In terms of geometry, apart from the feed conduit and discharge conduit, the body 102 mainly includes conical sections on the inflow and outflow sides and a substantially cylindrical intermediate section.

[0173] From a functional perspective, reactor 100 includes a distribution section 134, a mixing section 127, a reaction section 135, and a collection section 136. The inlet section 124 is arranged above the distribution section 134 on the inflow side, and the outlet section 138 is connected below the collection section 136 on the outflow side. Reactor 100 includes a first reactant conduit 119 for a first reactant, a second reactant conduit 120 for a second reactant, a feed conduit 140 for HTM, a product conduit 130 for discharging product or substrate containing product, and an outlet conduit 142 for the heat transfer medium. The function and channels of the individual sections and the conduit wiring will be described in more detail below with reference to partial view II and the accompanying drawings.

[0174] Reactor 100 also includes a plurality of sensor holders 152. Here, the sensor holders 152 are configured to receive sensors 150, which can be introduced into or held in a sensor base 154 or sensor channel by a mating sensor or measuring end. Hereinafter, sensor base 154 should generally be understood to mean guide and holder, which is arranged outside the body 102 and configured as a generally hollow guide tube with suitable fixing and / or clamping means. Figure 1 Inside the reactor 100 (not shown), the sensor base 154 has the following section within its interior 110:

[0175] - If a solid material is penetrated in the direction of sensor axis 156, the section is configured as an opening or cutout, and

[0176] - If it spans an internal cavity or internal channel, the section is configured as a guide tube.

[0177] Until reaching the defined measurement point 158 ​​in the interior 110 of the reactor 100, which serves as the defined end of the sensor base 154. In this case, even though it is not configured as a continuous “base” as described above, it is still consistently referred to as the “sensor base”. The sensor axis 156 corresponds to the axis of the sensor holder 152 / sensor base 154, and therefore the term “sensor axis” is interpreted accordingly in this case.

[0178] By way of example, this exemplary embodiment shows two sensors 150, each held in a sensor holder 152, wherein the measuring end (not shown) of the sensor or the respective sensor 150 is inserted into the corresponding measuring point 158. A total of four sets of three sensor holders 152 are arranged circumferentially in each case of the reactor 100. The measuring point 158 ​​of the sensor 150 is arranged in each case within the interior 110 and adjacent to the helical channels 210, 212, as described below, particularly in… Figure 6 and Figure 8 As shown in detail below. All sensors 150 are connected to the control unit 600 via data conduits as indicated by the dotted lines. The control unit 600 is used to receive measurement signals from the sensors 150 and may include electronic components, particularly microelectronic components, for processing, storing, and / or evaluating the measured signals, specifically including components for converting analog measurements into digital data.

[0179] In the illustrated examples, in each case, three sensors 150 arranged aligned with each other form a corresponding sensor group that monitors the internal channels at three height levels along the longitudinal axis 104. Thus, the measurement point 158 ​​of the first sensor group is assigned to different height levels of the external reaction channel 200 (see partial view II), the measurement point 158 ​​of the second sensor group is assigned to different height levels of the internal reaction channel 202, the measurement point 158 ​​of the third sensor group is assigned to different height levels of the external heat exchange channel 144, and similarly, the measurement point 158 ​​of the fourth sensor group is assigned to the internal heat exchange channels 145, 146, or 147 (see especially...). Figure 4 ).

[0180] In an exemplary embodiment of the invention, a sensor group monitors two of the internal spiral channels 210 of the external reaction channel 200 at different height levels. A first sensor group is arranged such that it monitors the first spiral channel 210 at the upper and lower positions and the third spiral channel 210 at the center position. A second sensor group is arranged such that it monitors the third spiral channel 210 at the upper and lower positions and the first spiral channel 210 at the center position.

[0181] The third and fourth sensor groups are arranged such that the helical channels 212 of the internal reaction channel 202 are monitored in a similar manner, wherein, for design reasons, three or four of the four helical channels 212 are monitored at different height levels. In this embodiment, the third sensor group monitors the first helical channel 212 at the upper and lower positions, and monitors the second helical channel 212 at the center position. The fourth sensor group monitors the upper and lower positions of the third helical channel 212, and monitors the fourth helical channel 212 at the center position.

[0182] The carrier element 107 is arranged at the height of the cylindrical reaction section 135 on the main body 102, through which the reactor 100 is mechanically fixed to the retainer and carrier unit (not shown). Any conventional temporary or permanent fixing components can be provided.

[0183] Partial View II shows the same reactor 100 as in Partial View I, but only in perspective plan view of the channels for the two reactants, reaction mixture, and products. In other words, Partial View II shows the liquid surface as a negative of the associated channels, and all wall structures are removed in this illustration. Furthermore, all conduits and internal channels for the heat transfer medium are not shown in Partial View II, namely the feed conduit 140, the discharge conduit 142, and all associated channels such as internal heat exchange channels 144, 145, and 146, and the spiral heat exchange channel 147.

[0184] In this document and following the accompanying drawings, references are made to "top," "side," "beside," and "bottom," or similarly, "above," "below," "horizontal," or "height." This type of description is for ease of illustration only and follows the example shown for reactor 100, which is shown in a vertical orientation and, in this example, traverses from top to bottom, and has reactant conduits 119, 120 arranged at the top and a product conduit 130 arranged at the bottom. In this document, the above-described type of description also relates to the flow direction of the medium in reactor 100 and, in the absence of any specific indication or contrary indication, is synonymous with the flow direction of the corresponding medium.

[0185] However, this should not be construed as restrictive in the absence of any specific instructions, as reactor 100 can be oriented in any orientation in principle, resulting in the longitudinal axis 104 being oriented horizontally or at an angle to the vertical direction of gravity, thereby similarly altering other configurations of elements, components, and orientations.

[0186] Two reactant conduits 119, 120 are routed in the inlet section 124, and may include suitable connecting elements (not shown), such as flanges, threads, or other elements, on the exterior of the body 102. In the distribution section 134, the reactant conduits 119, 120 include a distributor 122 and a diffuser 123. In the illustrated example, at least one distributor 122 is arranged upstream of the diffuser 123 in the respective reactant conduit 119, 120 in the flow direction F, resulting in the respective reactant conduits 119, 120 being divided into at least two (four in this case) conduit branches leading to subsequent distributor channels 112, 114. The diffuser 123 forms a transition / inlet channel section for introducing the respective reactant into the associated distributor channels 112, 114.

[0187] In the exemplary embodiment shown, the (primary) distributor channels 112, 114 are four annular channels arranged concentrically with each other, as particularly in combination Figure 3 and Figure 4 As described more specifically, a mixing section 127 is arranged below the dispenser channels 112, 114 and serves as a transition, through which the two dispenser channels 112, 114 for one of the reactants are connected and lead to the two secondary dispenser channels 129.

[0188] Each of the two secondary distributor channels 129 has a reaction channel 200, 202 connected thereto. The reaction channels 200, 202 are each configured as a multi-helix, each comprising four helical channels 210, 212. In other words, the reaction mixture present in the secondary distributor channel 129 is distributed onto the four helical channels 210 of the reaction channel 200 and discharged. In the case of a strongly exothermic reaction (e.g., alkoxylation), the reaction begins immediately after the reactants come into contact in the secondary distributor channel 129, such that the secondary distributor channel 129 has been partitioned into a reaction section 135 with associated cooling requirements.

[0189] Mixing section 127 is determined by the location of the transition and merging of the respective reactants that produce the reaction mixture, wherein the different reactants also continue to undergo, in particular, fluid-mechanical mixing in the secondary distributor channel 129. Mixing section 127 is the transition of reactor 100 from distribution section 134 to reaction section 135, and... Figure 1 The text shows an overlap with two recorded sections, and... Figure 2 , 3 The sections shown in Figures 1 and 6 are delimited by curly braces. This does not represent a different implementation, but rather illustrates the fluid transition from the distribution section 134 to the reaction section 135 within the region of the mixing section 127.

[0190] In this context, "multiple spirals" should be understood to mean a channel structure in which two or more channels are arranged in a spiral shape, are generally parallel to each other, and are spaced apart from each other in the vertical direction. The spiral channels of the multiple spirals are connected to a common secondary distributor chamber 129.

[0191] In an embodiment not shown, the secondary distributor chamber is a ring segment or comprises two or more ring segments, wherein at least two helical channels are connected to one ring segment. All helical channels of the secondary distributor chamber configured as a ring segment or all ring segments of the secondary distributor chamber form a common reaction channel.

[0192] like Figure 1 As shown in partial illustration II, an outer reaction channel 200 configured as a multi-helix surrounds an inner reaction channel 202 also configured as a multi-helix, wherein each of the two reaction channels 200 and 202 includes four helical channels 210 and 212.

[0193] For clarity, the four spiral channels 210, 212 are not individually provided with reference numerals, wherein when viewed in the cross-sectional plane in the circumferential direction, in the image plane, the first spiral channel 210, 212 is on the left-hand side and the third spiral channel 210, 212 is on the right-hand side, and these channels are shown as elongated, hole-like opening surfaces.

[0194] A collection section 136, comprising multiple collection channels 116, 117, and 119, is connected to a reaction section 135. Within collection channels 116 and 117, corresponding spiral channels 210 and 212 are merged and introduced into the product conduit 130. In the illustrated example, a collection unit 132 is arranged between the final collection channel 118 and the product conduit 130; this collection unit 132 also functions as a mixing and settling chamber.

[0195] At the lower end of the main body 102, a conical structure including two or four openings 160 is shown. These openings 160 represent areas in which the spiral heat exchange channels 147, in which the heat transfer medium is conducted, are radially guided outward, and where they are introduced or transitioned into a common collection channel 148 (not shown). Figure 2 , Figure 9 ).

[0196] Multiple different channels inside the reactor 110 Figure 2 This is evident in the illustration. Reactor 100 corresponds to the one described in Partial Description I. Figure 1 The reactor, and therefore the following content is especially not previously mentioned. Figure 1The components and functions described together. The central longitudinal axis 104 lies in the cross-sectional plane (xz plane). In the introduction section 124, reactant conduits 119 and 120 extend out of the cross-sectional plane and are therefore not fully shown. Figure 2 Specifically, individual sections of reactor 100, the locations of sections A to D, and their relationship to... Figures 3 to 10 Instructions Figures 3 to 10 It is shown in section form and in more detail according to Figure 2 Reactor 100.

[0197] Figure 3 The illustration shows, in the form of an enlarged partial view of the upper section (which includes the introduction section 124, the mixing section 127, and the distribution section 134), according to Figure 2 The reactor 100 (cross-sectional view (xz plane)). Reactant 1, flowing in via the first reactant conduit 119, is split into two annular distributor channels 112 via an internal channel, a splitter 122, and a diffuser 123. Reactant 2, flowing in via the second reactant conduit 120, is similarly introduced from above into the two annular distributor channels 114 via the partially shown internal channel, splitter 122, and diffuser 123. The introduction from above via the diffuser 123 is achieved outside the cross-sectional plane and is shown by dashed arrows. The four annular distributor channels 112, 114 are arranged concentrically and in pairs, such that the distributor channel 112 for conveying reactant 1 is always arranged adjacent to the distributor channel 114 for conveying reactant 2. In each case, the four pairs of distributor channels 112, 114 and the distributor channels 112, 114 are arranged concentrically relative to each other as a whole. A mixing section 127 is arranged below the distributor channels 112, 114. The mixing section 127 is primarily formed by a plurality of mixing channels 128 that form lower outlets from distributor channels 112, 114 and inlets to one of two secondary annular distributor channels 129. A pair of directly adjacent mixing channels 128 of distributor channels 112, 114 are arranged such that they lead to a common secondary distributor channel 129, whereby reactants 1 and 2 are mixed and the reaction begins in the subsequent distributor channel 129.

[0198] In the example shown, the mixing channel 128 alternately extends in the circumferential direction from each distributor channel 112, 114 to the downstream secondary (shared) distributor channel 129.

[0199] In each case, the two distributor channels 112, 114 containing unmixed reactants 1, 2 can also be referred to as primary distributor channels 112, 114, because they are passed through first.

[0200] The central feed duct 140 branches into internal heat exchange channels 143-147, which are configured as concentric annular heat exchange channels 144-146 and as a spiral heat exchange channel 147. In the distribution section 134, heat exchange channels 144-146 are configured as concentric annular channels similar to distributor channels 112, 114. In the reaction section 135, heat exchange channel 147 is configured as a spiral channel. Figure 5 The internal distribution includes multiple lateral distribution channels 143, one of which is located in the plane of the cross-section shown. (See figure) Figure 3 As shown, the central feed conduit 140 for the heat transfer medium branches directly into an outer annular heat exchange channel 144 and a transverse channel 143. The top of the transverse channel 143 is connected to and feeds into the central annular heat exchange channel 145 and the inner heat exchange channel 146. Thus, a pair of annular distributor channels 112, 114 have heat exchange channels 144-146, which are also arranged annularly on both sides. In other words, in each case, the two distributor channels 112, 114 (which form an adjacent pair and lead to a shared secondary distributor channel 129) for one of the two reactants have a shared partition wall and each has a wall shared with the adjacent heat exchange channels 144-146. The annular heat exchange channels 144-146 and the distributor channels 112, 114 / their pairs are concentrically surrounded by each other.

[0201] In the example shown, the heat exchange channel 144 is arranged radially outward, followed by two pairs of outer distributor channels 112, 114 in a radial direction toward the longitudinal axis 104, a central heat exchange channel 145 concentrically surrounding the two pairs of inner distributor channels 112, 114, and an innermost annular heat exchange channel 146 concentrically surrounded by the inner pairs of inner distributor channels 112, 114 and all other annular channels in this reactor section.

[0202] Another specific advantage discovered is that, on the one hand, the annular trough-shaped distributor channels 112, 114, and on the other hand, the similarly annular trough-shaped heat exchange channels 144, 145, 146, are concentrically arranged, allowing the fluid already present in the distribution section 134 to achieve heating and / or temperature equilibrium. In the test setup, reactants were supplied at a temperature of 15°C to 20°C, and HTM was supplied at a temperature of approximately 60°C. In the distribution section 134, the HTM had been cooled by approximately 20°C to 25°C, and the reactants in the distributor channels 112, 114 were heated by a considerable amount. As a result, the thermal regeneration of HTM requires less energy, and temperature equalization avoids stress in the reactor body. In other words, it has been very generally proven that for the reactor and the (synthetic) methods carried out there, it is advantageous for HTM (here, oil) to act as a heating medium that heats the cooler reactants and thereby accelerates the initiation / reaction of the reaction upstream of the distribution section 134. Downstream of distribution section 134, the mixture of substances present is hotter than HTM, which then acts as a coolant.

[0203] Figure 3 Further shown are inclined mixing channels 128, which are in the cross-sectional plane and extend from the bottom of the distributor channels 112, 114 into the corresponding common annular distributor channel 129.

[0204] Figure 4 This diagram shows a horizontal cross-sectional view (xy plane) of reactor 100 in distribution section 134 - this corresponds to Figure 2 Section AA is shown in the diagram. Sensor holders 152 are arranged on the outside of the body 102, four of which are fully shown in the top plan view, and another four are shown in cross-section. The sensor holders 152 are arranged aligned with each other along a path parallel to the longitudinal axis 104. The carrier element 107 is also shown in cross-section, and the lower discharge conduit 142 is shown in plan view. As already combined Figure 3 As explained, each pair of annular distributor channels 112, 114 has two identical annular heat exchange channels 144-146 arranged adjacent to it. This forms concentric channels in the following order from the outside to the inside: heat exchange channel 144, distributor channel 112, distributor channel 114 (first pair), central heat exchange channel 145, distributor channel 112, distributor channel 114 (second pair), and innermost heat exchange channel 146.

[0205] exist Figure 5 The illustration shows a horizontal cross-sectional view (xy plane) of reactor 100 at the height of mixing section 127, which corresponds to Figure 2 Section BB in the middle. On the outside of the main body 102, similar to Figure 4The illustration shows eight sensor holders 152, of which six are also shown in cross-sectional plane. The sensor holders 152 are arranged to be vertically aligned with each other along a path parallel to the longitudinal axis 104. Figure 5 Two secondary distributor channels 129, multiple mixing channels 128, and sensor bases 154 within the interior 110 are also shown. Mixing channels 128 are arranged closely together circumferentially on the inflow side of each secondary distributor channel 129, serving as outlets for the (primary) distributor channels 112, 114 (not shown) arranged above them. An external heat exchange channel 144 penetrated by sensor bases 154 is also shown in the upper left and lower right of the image plane, and a central heat exchange channel 145 is penetrated by two additional sensor bases 154, wherein the sensor bases 154 are specifically configured as guide channels or openings in the region of the central heat exchange channel 145. Thus, the sensor bases 154 form an integral mechanical structure within the interior 110 of the reactor 100.

[0206] Figure 6 The diagram is shown in the form of an enlarged partial view of the central section (reaction section 135). Figure 1 A cross-sectional view (xz plane) of reactor 100. Figure 6 The initial section includes a mixing section 127, a reaction section 135, and a collection section 136. An outer reaction channel 200 and an inner reaction channel 202 (as shown by the dotted line) are arranged in the reaction section 135, along with a heat exchange channel 147. The exemplary embodiment shown provides three heat exchange channels 147 arranged radially from the outside to the inside in the following order: heat exchange channel 147 (outer), reaction channel 200 (outer), heat exchange channel 147 (center), reaction channel 202 (inner), and heat exchange channel 147 (inner). The reaction channels 200 and 202 are configured as multiple spirals. The multiple spirals of the outer reaction channel 200 are formed by spiral channels 210, and the multiple spirals of the inner reaction channel 212 are formed by spiral channels 212. The heat exchange channel 147 is at least partially formed as a spiral channel in the reaction section 135. Thus, each reaction channel 200, 202 has adjacent spiral heat exchange channels 147 on both sides, and can be effectively cooled. On the inflow side, the spiral channel 210 of the outer reaction channel 200 is in fluid communication with the outer secondary distributor channel 129, and the spiral channel 212 of the inner reaction channel 202 is in fluid communication with the inner secondary distributor channel 129 and is fed from the inner secondary distributor channel 129.

[0207] In the vertical cross-sectional plane (xz plane), the helical channels 210, 212 have a rectangular or nearly rectangular cross-section, wherein the height is along the direction of the longitudinal axis 104, and the width is radially or transversely to the longitudinal axis 104. In the exemplary embodiment shown, the short side is shown as a radius and the long side is shown as substantially straight. The ratio of the width B to the height H of surface A is selected under the desired process conditions such that laminar flow is formed in the helical channels 210, 212. The Reynolds number Re is defined by the following quotient:

[0208] Re = ρ v L / µ.

[0209] Here, ρ = fluid density, v = flow velocity, L = characteristic length, and µ = fluid viscosity. Re is advantageously no greater than 9000. Region A in the cross-sectional plane (xz plane) differs from the channel cross-section transverse to the main flow direction in the helical channels 210, 212, where a similar distinction is necessary if the influence is correspondingly large (e.g., in the case of a very strong inclination of the helical channels 210, 212, making region A in the cross-sectional plane not equivalent to the flow cross-section). If in doubt, the flow cross-section will be used for the configuration of the geometry.

[0210] In the cross-sectional plane (xz plane), the helical channel 147 has a cross-section that is generally rectangular, trapezoidal, or parallelogram-shaped, at least along a portion of its length in the reaction section 135. It has proven advantageous that the cross-section W1 of the central heat exchange channel 147 has at least 1.3 times the surface area, and particularly at least 2 to 5 times the surface area, compared to the cross-section W2 of the innermost or outermost heat exchange channel 147.

[0211] The significant advantage of the dual and parallel winding of heat exchange channel 147 and reaction channels 200, 202 / spiral channels 210, 212 is that optimal cooling of the highly exothermic reaction mixture is possible, and hot spots are always avoided. This ensures the safe prevention of combustion of the reaction mixture and comprehensively improves and homogenizes product quality.

[0212] Furthermore, reactor 100 is optimally monitored via multiple sensors 150 arranged along the flow path and is controllable via control unit 600. If an unfavorable temperature distribution is detected in the reaction sections of reaction channels 200, 202 or the helical channels 210, 212 monitored by the sensors, the reaction can be selectively affected, for example, by reducing the volumetric flow rate of at least one reactant stream and / or heat transfer medium.

[0213] exist Figure 7 The illustration shows a horizontal cross-sectional view (xy plane) of reactor 100 at a height of 135 in the central reaction section - this corresponds to Figure 2 Section CC in the middle. Figure 7 The four external spiral channels 210 of the external reaction channel 200 are shown. Figure 6 The four horizontal cross-sections of the internal reaction channel 202 and the four spiral channels 212 ( Figure 6 The four horizontal cross-sectional areas of the ) and the four horizontal cross-sectional surfaces of each of the three spiral heat exchange channels 147. (As from...) Figure 6 and 7 As clearly shown in the cross-sectional diagram, the heat exchange channel 147 is advantageously helical, and thus follows the helical structure of helical channels 210, 212, in which the reaction essentially takes place. However, the geometry and dimensions of the cross-sections of the helical channels 210, 212 and the helical heat exchange channel 147 differ from each other. The helical heat exchange channel 147 is optimized to achieve optimal heat dissipation. Figure 7 Two opposing measurement points 158 are shown as examples of the four internal spiral channels 212. For this purpose, a sensor base 154 is configured as a sensor guide or opening in a region of solid material or wall, and spans the central heat exchange channel 145 as a base. The two measurement points 158 illustrated are arranged at a height within the reaction section 135, in each case immediately adjacent to one of the internal spiral channels 212.

[0214] Figure 8 The lower end of the reaction section 135, the collection section 136, and the discharge section 138 of the reactor 100, as well as the outlet side 108 of the reactor 100, are shown in a vertical cross-sectional view (xz plane). In the flow direction F, the reaction section 135 transitions into the collection section 136, to which the discharge section 138 connects. In the collection section 136, a spiral heat exchange channel 147 and annular or conical collection channel 148 are cascaded with conduits until all heat exchange channels 147 and collection channels 148 are merged into the lowermost collection channel 149, thereby consolidating the heat transfer medium into a single flow. The lowermost connecting channel 149 connects to the discharge conduit 142, through which the heat transfer medium can be discharged from the interior 110 of the reactor 142.

[0215] In a similar manner, spiral channels 210 and 212 are incorporated into the cascaded end (product) collection channels 116 and 118. Figure 8In the depicted exemplary embodiment, the groups of four spiral channels 210, 212 of the respective reaction channels 200, 202 each lead to a corresponding annular (product) collection channel 116, and these channels merge downstream into a common (product) collection space 118. This common (product) collection space 118 can, in principle, have any geometry, and is advantageously annular, conical, or a combination thereof. Similarly, the outer (product) collection channel 116 has an upper annular section parallel to the longitudinal axis 104 and a lower conical section leading downstream into the common collection space 118.

[0216] Downstream of the lowest collection space 118, Figure 8 An exemplary embodiment further illustrates a discharge chamber 137, which is in the form of an inner chamber with a radially expanding interior. This discharge chamber 137 provides an extended residence time for the product mixture, thereby homogenizing and calming the flow in terms of pressure. The discharge chamber 137 includes: a top region that conically widens in the flow direction F; a substantially cylindrical, elongated central region; and a conically narrowing outflow section or bottom section. The outflow side of the discharge chamber 137 is connected to the product conduit 130. Any desired fixing members or sections on the discharge conduit 142 and the product conduit 130 are not shown.

[0217] exist Figure 9 The diagram shows a horizontal cross-sectional view (xy plane) of reactor 100 at the height of collection section 136—this corresponds to... Figure 2 The DD section is shown in the cross-sectional plane. In the cross-sectional plane, the channels are presented as four concentric rings, with two (product) collection channels 116 arranged radially between two collection channels 148 for the heat transfer medium. Thus, the cross-sectional plane DD is above the corresponding final collection channels 118, 149. Example measurement

[0218] According to Figures 1 to 9 In an exemplary embodiment, the reactor 100 described above is used to perform alkoxylation of propylene oxide C3H6O (reactant 1) and chain initiator allyl C2H6O2 (reactant 2) with a liquid polymetallic cyanide complex catalyst that has been mixed with reactant 2.

[0219] Addition reactions can be described as follows:

[0220] C2H6O2 + C3H6O → C5H12O3

[0221] C5H12O3 + C3H6O → C8H18O4

[0222] …

[0223] C11H24O5 + C3H6O → C14H30O6

[0224] The reactor and process conditions have the following data:

[0225] The internal secondary distributor channel 129, in the form of a ring channel, has an inner diameter of 11.8 mm and an outer diameter of 14.2 mm (channel width 2.4 mm) and a diameter of 4.21 mm. -6 Local flow rate of kg / s.

[0226] The external secondary distributor channel 129, in the form of a ring channel, has an inner diameter of 32.6 mm and an outer diameter of 35 mm (channel width 2.4 mm) and an 8.25 e -6 The local flow rate is approximately twice the flow rate of the internal distributor channel, which is kg / s.

[0227] Each of the corresponding reaction channels 200 and 202, each having four helical channels 210 and 212, is connected to two secondary distributor channels 129. The vertical cross-section A (xz plane) of the helical channel 210 of the inner reaction channel 202 has a height H of 3.29 mm and a width B of 1.2 mm in the z-direction. For the outer reaction channel 200, the height H in the xz plane is 5.3 mm and the width B is also 1.2 mm.

[0228] The horizontal cross section A2 (xy plane) of the spiral channel 210 of the internal reaction channel 202 has a length L of 3.42 mm and a width B of 1.2 mm in the circumferential direction. For the external reaction channel 200, the horizontal cross section A2 has a length L of 12.072 mm and a width B of 1.2 mm in the circumferential direction.

[0229] • The flow rate in the corresponding four spiral channels downstream of the secondary distributor channel 129 is ¼ of the above value.

[0230] The heat exchange medium used is heat exchange oil.

[0231] The reactor has a total of 12 sensor holders, including 12 sensors, all of which are designed as temperature sensors and are connected to the control and evaluation unit via data transmission.

[0232] The reactor used in the exemplary embodiment has the following dimensions:

[0233] - Total height 340 mm

[0234] - The diameter of the pressure-bearing area is 56 mm.

[0235] The experimental conditions are shown in the table below:

[0236] In the region of the secondary distributor channel and in the subsequent inflow through spiral channels 210, 212, the temperature in reactor 100 reaches a maximum of 200.7°C. This is a non-critical hotspot that does not adversely affect product quality. Reactor 100 operates continuously under these conditions for a period of time.

[0237] Considering the flow rate of the present invention of approximately 0.58 mm / s, the reaction mixture is subjected to this temperature of approximately 200°C for approximately 5.16 seconds over a distance of only approximately 3 to 5 mm in the region of the secondary distributor channel and during the inflow into the helical channel. After approximately 10% to 15% of the length of the helical channel, the temperature of the reaction mixture measured at the wall of the helical channel reaches a value of less than 136°C. At the end of the helical channel, values ​​of approximately 85°C to 92°C are continuously obtained. The geometry of reactor 100, and particularly the helical channels 210 and 212, ensures that, without any backmixing, no part or molecule is subjected to the maximum process conditions for a longer period than described above.

[0238] It was demonstrated that product quality was achieved or improved in every aspect throughout the entire synthesis duration. The consistent flow and process conditions defined within a narrow parameter window enabled the achievement of higher product purity, particularly improved uniformity and reduced turbidity.

[0239] Compared to stirred reactors, the improved conversion, with its lower tendency to form byproducts, makes it possible to improve the ratio of reactant to product (kg).

[0240] Figure 10 A highly schematic apparatus 500 for producing products using reactor 100 is shown, wherein reactor 100 includes a first reaction section similar to the reactor 100 described above and a plurality of reaction channels 200, 202 arranged concentrically to each other and configured as multiple helices.

[0241] A second reaction section 350, configured as a straight reaction tube 300, is connected to the first reaction section 135. A separation unit 400 is arranged downstream of the reaction tube 300. In one embodiment of the method and apparatus, the dominant pressure in the reaction tube 300 is the same as or substantially the same as the pressure in the first reaction section 135 (not shown) of the reactor 100, where minute cooling or heating may be provided. All reaction mixtures from two or more helical channels 210, 212 are combined in the reaction tube 300. The already very calm reaction (now only slightly exothermic, if any) continues until the desired conversion is achieved. In the exemplary embodiment shown, the flow path of molecules in the reaction section 135 of the reactor 100 in the main flow direction (flow direction F) is in the range of 0.25 to 0.35, based on the total distance traveled up to the outlet from the reaction tube 300. The total distance is determined from the end of the mixing section or the beginning (upper end) of the secondary distributor channel 129 until at least 95% conversion relative to the desired product or desired conversion is achieved. Reactor 100 and reaction tube 300 are shown as being located on an axis, wherein these may also be arranged differently, such that... Figure 10 In an embodiment not shown, the reactor 100 is arranged vertically and the reaction tube 300 is arranged horizontally, with a suitable curved transition provided between the two parts.

[0242] A controllable throttle valve 302 is further provided in the product conduit 130, which is connected to and controlled by the control unit 600 via data transmission.

[0243] Separation unit 400 includes an outlet conduit 402 for the product or product mixture and a gas discharge conduit 404 for volatile substances from the product or product mixture. Separation unit 400 achieves a pressure reduction in the reaction zone from about 30 to 40 bar (p1) to about 1 bar (p2), without further detail. Volatile substances are thus separated in a known manner.

[0244] Reference Symbol List

[0245] 100 reactors

[0246] 102 Main Body / Shell

[0247] 104. Longitudinal axis (z-axis)

[0248] 106 Inflow side

[0249] 107 Carrier Components

[0250] 108 Outflow side

[0251] 110 Internal

[0252] 112 Distributor Channels

[0253] 114 Distributor Channels

[0254] 116 Collection Channel

[0255] 117 Collection Channel

[0256] 118 Collection Channel

[0257] 119 Reactant conduit

[0258] 120 Reactant Conduit

[0259] 122 splitter

[0260] 123 Amplifier

[0261] 124 Introduction Section

[0262] 127 Mixed Section

[0263] 128 Mixed Channels

[0264] 129 Distributor Channel (Secondary)

[0265] 130 Product delivery tube

[0266] 132 Collection Units

[0267] 134 Allocation Section

[0268] 135 Reaction Section

[0269] 136 Collection Section

[0270] 137 Exhaust Chamber

[0271] 138 Discharge Section

[0272] 140 Feed pipe

[0273] 142 Discharge catheter

[0274] 143 Horizontal Channel

[0275] 144 Heat exchange channel (external)

[0276] 145 Heat Exchange Channel (Center)

[0277] 146 Heat exchange channel (internal)

[0278] 147 Heat exchange channel (spiral)

[0279] 148 Collection Channels

[0280] 149 Collection Channel

[0281] 150 sensors

[0282] 152 Sensor Holder

[0283] 154 Sensor Base / Channel

[0284] 156 Sensor axis

[0285] 158 measurement sites

[0286] 160 opening

[0287] 200 reaction channels, multiple helices

[0288] 202 Reaction Channel, Multiple Helices

[0289] 210 Spiral Channel

[0290] 212 Spiral Channel

[0291] 300 reaction tube

[0292] 302 Throttling Valve

[0293] 350 reaction zone, second

[0294] 400 Separation Unit

[0295] 402 Discharge catheter

[0296] 404 gas discharge conduit

[0297] 500 devices

[0298] 600 control unit

[0299] A cross section

[0300] F Flow direction

[0301] The W transverse region, also known as W1 and W2.

Claims

1. A reactor (100) for carrying out a synthetic method for producing a product from at least two reactants, comprising: a. The main body having a longitudinal axis (104), an inflow side (106), and an outflow side (108); b. Internal (110); c. At least two reactant conduits (119, 120), each of which is connected to at least one dispenser channel (112, 116) on the inflow side; d. At least one product conduit (130) connected to at least one collection channel (116) on the outflow side; e. At least one distribution section (134) comprising at least two distributor channels (112, 116) and at least one splitter (122); f. At least one mixing section (127), wherein at least two dispenser channels (112, 116) are connected via a mixing channel (128) and at least two reactants are combinable; g. At least one reaction section (135) comprising at least one reaction channel (200, 202); h. At least one collection section, which includes at least one collection channel (116); i. At least one inflow-side feed conduit (140) for the heat transfer medium to enter the interior (110); and at least one outlet conduit (142) for the heat transfer medium to exit the interior (110), wherein - The heat transfer medium may flow around at least a portion of the length of at least one reaction channel (200, 202) in the interior (110), and / or - At least one heat exchange channel is provided in which the heat transfer medium can flow, wherein the at least one sub-section is arranged adjacent to the at least one reaction channel (200, 202), and wherein the at least one heat exchange channel (147) and the at least one reaction channel (200, 202) are separated from each other by a common channel wall. The feature is that the at least one reaction channel (200, 202) is a multiple spiral comprising two or more spiral channels (210, 212), wherein on the inflow side, each spiral channel (210, 212) of the multiple spiral is connected via the at least one mixing section (127) to at least one distributor channel (112, 114) of each of the at least two reactants, and wherein on the outflow side, each spiral channel (210, 212) of the multiple spiral is connected to at least one collection channel (116).

2. The reactor according to claim 1, characterized in that, The reactor comprises two or more reaction channels (200, 202) as multi-helices, wherein the outer multi-helices of the outer reaction channel (200) concentrically surround at least the inner multi-helices of the inner reaction channel (202), and wherein each reactant conduit (119, 120) is directly or indirectly connected to each multi-helice.

3. The reactor according to claim 1 or 2, characterized in that, The inflow side of each reaction channel (200, 202) configured as a multi-helix is ​​connected to a dedicated distributor channel (112, 114, 129) and / or a mixing section (127).

4. The reactor according to any one of the preceding claims, characterized in that, At least one additional distributor channel (129) and / or an inlet to each spiral channel (210, 212) is arranged downstream of at least one inflow-side distributor channel (112, 114) in the direction of the longitudinal axis (104).

5. The reactor according to any one of the preceding claims, characterized in that, The outflow side collection channel (116) is connected to the outlet throttle valve and / or the outlet nozzle and / or includes the throttle valve and / or the nozzle.

6. The reactor according to any one of the preceding device claims, characterized in that, The minimum width of the cross section (A) of the spiral channel (210, 212) is 0.8 mm to 3 mm, ideally 0.8 mm to 2 mm.

7. The reactor according to any one of the preceding claims, characterized in that, The cross section (A) in the spiral channel (210, 212) has an elliptical, oval, or at least approximately rectangular basic structure, wherein the ratio of the minimum width (B) to the maximum length (H) of the cross section is advantageously not less than 0.5, ideally in the range of 0.2 to 0.

06.

8. The reactor according to any one of the preceding device claims, characterized in that, At least one sensor holder (152) is provided for accommodating and / or fixing a sensor (150), wherein the sensor holder (152) includes a sensor base (154) which is connected at one end to a helical channel (210, 212) in the interior (110) and passes through the interior (110) and through the reactor wall of the body (102), and wherein the sensor (150) accommodating and / or fixing is external to the body (102) and can be connected to a data receiver in a data conduction manner.

9. The reactor according to any one of the preceding claims, characterized in that, Each reaction channel (200) or a spiral channel (210, 212) of each reaction channel (200) has a sensor base (154) leading to its sensor holder (152), and specifically, a plurality of sensor bases (154) are arranged in the direction of the longitudinal axis (104).

10. The reactor according to any one of the preceding device claims, characterized in that, Each individual spiral channel (210, 212) has at least one sensor base (154) leading to it, and specifically, each reaction channel (200, 212) has at least two sensor bases (154) leading to it.

11. The reactor according to any one of the preceding device claims, characterized in that, The interior (110) includes at least two separate heat exchange spaces or channels (144) and / or groups of heat exchange channels, which are fluidly and spatially separated from each other by at least one separating element (146) and / or section of the interior (110), wherein each heat exchange space or channel (144, 146) has at least one inlet conduit (140) and one outlet conduit (142), and each heat exchange space or channel (144, 146) can utilize different heat transfer media and / or operate at its own temperature level.

12. The reactor according to claim 11, characterized in that, The separating element (146) includes an insulating layer and / or is at least partially made of an insulating material.

13. The reactor according to any one of the preceding device claims, characterized in that, The main body has a protective shell arranged around it.

14. The reactor according to claim 13, characterized in that, The protective housing includes an extraction, filtration, and / or absorption unit and / or is connectable to the extraction, filtration, and / or absorption unit.

15. The reactor according to any one of the preceding device claims, characterized in that, Downstream of at least one inflow-side distributor channel (119, 120), in the direction of the longitudinal axis, at least one spiral channel (210) of the first reaction channel (200) merges with at least one spiral channel (212) of another reaction channel (202), and in particular, each spiral channel (210) of the first reaction channel (200) merges with a corresponding different spiral channel (212) of the other reaction channel (202).

16. The reactor according to any one of the preceding device claims, characterized in that, Downstream of at least one inflow-side distributor channel (119, 120), in the direction of the longitudinal axis, spiral channels (210, 210) of at least two reaction channels (200, 202) enter a common reaction tube (300) via a collection unit (132), specifically into a common reaction tube (300) sized such that the residence time of the reaction mixture in the reaction tube (300) is... - Corresponding to at least 50% of the total reaction duration, specifically - Corresponding to at least 75% of the total reaction duration.

17. Apparatus (500) for a synthetic method of producing a product from a strongly exothermic reaction of at least two reactants, particularly liquid reactants, comprising at least one reactor (100), Its features are, The at least one reactor (100) is configured according to any one of claims 1 to 16.

18. The device (500) according to claim 17, characterized in that, It includes at least two reactors (100) configured in parallel as described in any one of claims 1 to 16.

19. The device according to any one of claims 17 or 18, characterized in that, At least two reactors (100) are connected on the outflow side to at least one common reaction tube (300), specifically to a common reaction tube (300) sized such that the residence time of the reaction mixture is... - Corresponding to at least 50% of the total reaction duration, specifically - Corresponding to at least 75% of the total reaction duration.

20. The device according to any one of claims 17 to 19, characterized in that, Downstream of the at least one reactor (100), the product conduit (130) is connected to a degassing unit, wherein the degassing unit includes... the following: - Product conduit (130) serving as feed conduit, - A first discharge conduit (402) for the product and / or a mixture of substances containing the product, and - Gas discharge conduit (404) for volatile substances, wherein The degassing unit is configured such that the pressure (p2) in at least a section within the degassing unit is no greater than 2 bar, preferably no greater than 1 bar, and especially a vacuum of up to 0.5 bar.

21. A method for producing a reactor (100) for synthesizing a product, characterized in that, The reactor (100) is configured according to any one of claims 1 to 16, and the reactor (100) is manufactured by means of: - Computer-implemented processes, and - Additive manufacturing process (AMP) via additive manufacturing apparatus (AMA).

22. The production method according to claim 21, characterized in that, The AMP is a laser-induced, powder bed-based melting process.

23. The production method according to claim 21 or 22, characterized in that, The computer-implemented process includes the following steps: a) Provide process data and design parameters for CAD software. b) Design data are determined via the CAD software, preferably using at least one strength determination, and particularly via calculations and / or simulations based on the FEM. c) Provide control data for additive manufacturing equipment. d) Producing the reactor (100) via the AMA.

24. A storage medium comprising at least one executable program code for performing the production method according to any one of claims 21 to 23 and / or controlling the AMA to perform the production method according to any one of claims 21 to 23.

25. The storage medium according to claim 24, characterized in that, The medium is a storage medium integrated into the AMA or connected to or potentially connected to the AMA via data transmission.

26. A synthetic method for producing a product by means of a chemical reaction, comprising the following steps: a) Provide at least one reactor; b) Provide the first liquid reactant; c) Provide a second liquid reactant, wherein the second reactant may be a substrate containing or containing a catalyst; d) Provide a liquid heat transfer medium; e) Continuously supply the first reactant, the second reactant, and the heat transfer medium to the reactor; f) In the mixing section (127) of the reactor (100), the first liquid reactant and the second liquid reactant are continuously mixed to obtain a liquid reaction mixture; g) Downstream of the mixing section (127) and inside the reactor (100), a liquid product mixture is continuously provided by reacting reactant 1 with reactant 2, and in particular with the reaction products, and wherein, by means of the reactor (100), at least a portion of the heat of reaction generated during the reaction is transferred from the reaction mixture and / or the product mixture to the heat transfer medium. h) Continuously remove the product mixture from the reactor; i) Continuously remove the heat transfer medium from the reactor. Its features are, The reactor (100) is configured according to any one of claims 1 to 16 and / or the method is carried out using the equipment according to any one of claims 17 to 20.

27. The synthesis method according to claim 26, characterized in that, Prior to step e), a third reactant (reactant 3) comprising at least one catalyst or being a catalyst itself is provided, and wherein in step f), the reactants are mixed continuously, simultaneously or substantially simultaneously.

28. The synthesis method according to any one of claims 26 to 27, characterized in that, The (process) pressure (p1) of the reactants is in the range of 10 bar to 100 bar, advantageously in the range of 20 bar to 80 bar, and ideally in the range of 35 bar to 65 bar.

29. The synthesis method according to any one of claims 26 to 28, characterized in that, The method includes strongly exothermic reactions, particularly reactions that release at least 70 kJ per mole of reactant 1, preferably at least 80 kJ per mole of reactant 1, and particularly reactions that release 85 kJ to 150 kJ per mole of reactant 1.

30. The synthesis method according to any one of claims 26 to 29, characterized in that, The reaction in the reactor (100) does not form volatile byproducts, and in particular, does not form volatile byproducts that require continuous removal, especially those that require continuous distillation removal.

31. The synthesis method according to any one of claims 26 to 30, characterized in that, The reaction is selected from the group consisting of: a. (polymer) addition, b. Polymerization of monomers containing carbon double bonds (C=C double bonds) c. Oxidation of organic compounds d. Esterification, e. Beckmann rearrangement for the synthesis of carboxamides.

32. The synthesis method according to claim 31, characterized in that, a. The (poly)addition is selected from the group consisting of: alkoxylation, preparation of 3-hydroxypropionitrile from HCN and ethylene oxide, preparation of polyurethane from isocyanate with alcohol or amine, addition reaction of carboxylic acid or carboxylic ester on epoxide, hydrogenation, hydrogenation silylation or hydroformylation. b. Polymerization of monomers having carbon double bonds (C=C double bonds), especially free radical polymerization, selected from the group consisting of: polymerization of acrylates, methacrylates, styrene and vinyl compounds, polymerization of butadiene and production of polybutadiene; c. Oxidation is selected from the group of reactions below: - Epoxidation of olefins - The following oxidation From isobutane to tert-butyl hydroperoxide, from methanol to formaldehyde, Propylene to acrolein, acrolein to acrylic acid, ethylene to acetaldehyde, Acetaldehyde to acetic acid, ethylene to acetic acid From cyclohexane to adipic acid, - Halogenation, - Chlorosulfonation, - Nitrification, - Bayer-Villiger oxidation, and - Andrewsoff Method.

33. The synthesis method according to any one of claims 31 or 32, characterized in that, The reaction is an alkoxylation reaction used to produce alkoxylated compounds, wherein... a) The first liquid reactant is an epoxide selected from the group consisting of: ethylene oxide (EO), propylene oxide (PO), 1-epoxide butane (BO), and phenyl ethylene oxide (SO); b) The second liquid reactant is a substrate / compound selected from the group consisting of alcohols, fatty alcohols, phenols, alkylphenols, amines, carboxylic acids and their esters, thiols and imidazolines, and wherein the catalyst is in particular a polymetallic cyanide complex catalyst, or an alkali metal or alkaline earth metal hydroxide, particularly sodium hydroxide, potassium hydroxide and cesium hydroxide, or a basic catalyst, such as an alkali metal alkoxide, particularly sodium methoxide and potassium methoxide, or a tertiary amine.

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