Reactor, plant and process for synthesis of products by strongly exothermic reactions

Abstract

Reactor for performing a synthesis process for producing products from at least two reactants comprising a main body having a longitudinal axis, an inflow side and an outflow side; an interior; at least two reactant conduits, each connected at the inflow side to at least one distributor channel; at least one product conduit connected at 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 flow splitter; at least one mixing section in which via mixing channels at least two distributor channels are connected and at least two reactants are combinable; at least one reaction channel; at least one collection section comprising at least one collection channel; at least one inflow-side feed conduit for a heat transfer medium into the interior and at least one discharge conduit for the heat transfer medium out of the interior, wherein the heat transfer medium can flow around at least a partial 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 this at least one subsection is arranged adjacent to the at least one reaction channel and wherein at least one heat exchange channel and at least one reaction channel are separated from one another by a common channel wall, wherein the at least one reaction channel is a multiple helix which comprises two or more helix channels, wherein at the inflow side each helix channel of a multiple helix is connected via the at least one mixing section to at least one distributor channel of each of the at least two reactants and wherein at the outflow side each helix channel of a multiple helix is connected to at least one collection channel.

Description

[0001] Reactor, plant and process for synthesis of products by strongly exothermic reactions

[0002] The present invention relates to a reactor and to a process for producing products in a strongly exothermic reaction of two or more reactants and to a production process for the reactor using a computer-implemented process and an additive manufacturing process.

[0003] A strongly exothermic reaction is, for example, an alkoxylation in which a chain initiator (reactant 2) is catalytically reacted with at least one alkylene oxide (reactant 1) to afford an alkoxylate. Suitable chain initiators include compounds (reactant 2) having a reactive hydrogen atom such as for example alcohols, fatty alcohols, phenol, alkyl phenols, amines, carboxylic acids and esters thereof, mercaptans and imidazolines.

[0004] Alkylene oxides (reactant 1) employed especially include ethylene oxide (EO) and propylene oxide (PO) and also 1 -butylene oxide (BO) and styrene oxide (SO). Alkoxylation with ethylene oxide is also known as ethoxylation. Repeated ethoxylation of fatty alcohols affords fatty alcohol polyethylene glycol ethers, which have a very wide variety of applications, including as surfactants and emulsifiers. Ethoxylation of fatty alcohols is therefore carried out industrially.

[0005] In industry, alkoxylation is carried out both in a batch process and continuously. In a batch process a limited batch quantity of substrate, alkylene oxide and catalyst is initially charged in a reaction vessel and the reaction performed therein. After completion of the reaction the alkoxylate is withdrawn from the reaction vessel. The batch process mode is especially employed in the production of small quantities (specialty chemicals).

[0006] For larger amounts, continuous operating modes are employed where the reactants are continuously introduced into a reactor, reacted therein and the product is continuously withdrawn. The so-called continuous reactor thus employs a continuous flow process.

[0007] In the production approach of microreaction technology in specialty chemicals, the reactants are likewise reacted continuously but with markedly lower mass flows so that smaller product quantities are ultimately produced than in classical continuous processes. The advantage of microreaction technology is a higher process intensity, which enables better controllability of the reaction, promises higher energy efficiency and requires less installation space for the equipment. In particular, microreaction technology allows better heat removal compared to batch processes since the same amount of substance is reacted in a small reaction space spread over a longer period.

[0008] By contrast, batch processes comprise reacting the same amount of substance in a large reaction space in a short time so that the heat of reaction must be removed from the reaction space over long distances. This always carries the risk of thermal hotspots inside the batch reactor, which favour the formation of unwanted byproducts. By contrast, the better thermal management of microreaction technology avoids hotspots so that unwanted side reactions are suppressed and a better product quality is ultimately obtained.

[0009] An introduction to microreaction technology is provided in:

[0010] Ehrfeld, W., Hessel, V., Lowe, H.: Microreactors: New Technology for Modern Chemistry, published online 29 April 2004, Wiley-VCH Verlag GmbH, DCI:10.1002 / 3527601953.

[0011] US 2006 / 045828A1 discloses a reactor having a plurality of reaction zones containing a catalyst for catalytic conversion of a feed stream. This produces a product stream, wherein each reaction zone is formed by a multiplicity of spiral-shaped reaction tubes in coaxial arrangement which have a compact, coil-like structure, wherein the reactor is proposed especially for the catalytic reaction of a methane steam reforming. The plurality of heat exchanger tubes connects the reaction tubes of the different reaction zones, wherein these have a spiral-shaped configuration.

[0012] EP2603543B1 discloses a microreaction process for production of polyether alcohols. EP 3 603 795 A1 discloses a reactor for continuous reaction of two reactants. This document suggests introducing a second reactant from a second channel via apertures spaced apart from one another into a reaction channel which is traversed by a first reactant and is arranged in the reactor interior in a self-supporting manner and can have a cooling medium flow around it in order to form a reaction mixture. The channels and in particular the reaction channel are simultaneously subjected to a flow of a cooling medium flowing around them. The disadvantage of this reactor and the reaction associated therewith is that the throughput performance is severely limited and the reaction in the reaction sector is controllable only with difficulty, if at all. The latter has an adverse effect on the product.

[0013] It is accordingly the object of this invention to provide a reactor and an accompanying manufacturing process which largely overcome the recited disadvantages.

[0014] The object is achieved in accordance with the invention by a reactor according to the features of Claim 1 and a plant according to the features of Claim 17, wherein the reactor is producible by a production process according to the features of Claim 21 . The object is moreover achieved in terms of a strongly exothermic synthesis reaction according to the features of Claim 26.

[0015] The reactor according to the invention is used to perform a synthesis process for producing products from at least two reactants and comprises

[0016] - a main body having a longitudinal axis, an inflow side and an outflow side; an interior; at least two reactant conduits, each connected at the inflow side to at least one distributor channel; at least one product conduit connected at the outflow side to at least one collection channel; at least one inflow-side distribution section comprising at least two (primary) distributor channels and at least one flow splitter in at least one of the reactant conduits, in particular in all reactant conduits; at least one mixing section in which via mixing channels the at least two distributor channels are connected and at least two reactants are combinable, in particular combinable in a downstream secondary distributor channel; a reaction section comprising at least one reaction channel, in particular two or more reaction channels; at least one collection section comprising at least one collection channel;

[0017] (at least) one inflow-side feed conduit for a heat transfer medium into the interior and (at least) one discharge conduit for the heat transfer medium out of the interior, wherein the heat transfer medium can flow around at least a partial 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 this at least one subsection is arranged adjacent to the at least one reaction channel and wherein at least one heat exchange channel and at least one reaction channel are separated from one another by a common channel wall.

[0018] The at least one reaction channel here is a multiple helix which comprises two or more helix channels, wherein at the inflow side each helix channel of a multiple helix is connected via the at least one mixing section to at least one distributor channel of each of the at least two reactants, and wherein at the outflow side each helix channel of a multiple helix is connected to at least one collection channel.

[0019] The reactor is particularly suitable for producing a product via a strongly exothermic reaction which is carried out in a liquid reaction mixture / between liquid reactants. The reactor is especially configured here to be able to employ liquid reactants which are gaseous under atmospheric conditions and, as a consequence of pressure, are present in a liquid phase in at least one reactant conduit or in the reactor.

[0020] The main body is advantageously elongate and comprises the interior. The term "interior” is not intended to be understood in a limiting manner and describes the volume enclosed by the main body. The interior can include solid material, cavities, channels etc. The interior can also be divided or segmented into two or more sections.

[0021] A primary distributor channel is to be understood as meaning a channel into which a reactant, reactant mixture or reactant stream is introduced in order subsequently to be distributed over a plurality of, for example, downstream channels arranged in the circumferential direction, in particular mixing channels. The primary distributor channel as yet has no reaction or substantially no reaction occurring therein, in particular not the main reaction for production of the desired product.

[0022] A secondary distributor channel is to be understood as meaning a channel in which at least two reactants, reactant mixtures and / or reactant streams from for example two primary distributor channels are introduced so that the main reaction directly commences in the secondary distributor channel. The mixing section typically forms the transition from the primary distributor channels to a secondary distributor channel.

[0023] The reactant conduits and also the product conduit may be provided with known securing means, such as flanges, threads etc. Furthermore the terms "on the inflow side", "on the outflow side", “inflow side”, “outflow side”, “top”, “bottom” etc. are not to be interpreted in a narrow sense and mean a rough arrangement, direction or orientation, so that they can also mean “in proximity to”.

[0024] The helix channels of a multiple helix are ideally coiled in the same direction and advantageously run parallel to one another along the majority of their extent. In other words, the helix channels of a multiple helix have identical or substantially identical inclination angles. Having regard to a vertically aligned longitudinal axis of the reactor the flow axis of a helix channel is advantageously inclined by 15° to 45° relative to the horizontal. In the case of a differently aligned longitudinal axis the inclination of the flow axis is derived analogously.

[0025] Depending on the outer radius of a multiple helix this may especially comprise 3 to 10 helix channels, in particular 3 to 6 helix channels. At the transition from the upstream distributor channel to the respective helix channel the helix channels advantageously have an inlet cone which narrows in the flow direction. In an advantageous variant this inlet cone comprises inlet flanks of different widths and angles, wherein the lower inlet flank in the main flow direction is flatter and for example at least along a subsection is aligned parallel to the flow axis of the respective helix channel and the upper inlet flank is steeper and / or has a smaller radius.

[0026] In one embodiment of the reactor, it may be advantageous when said reactor comprises two or more reaction channels as a multiple helix, wherein an outer multiple helix of an outer reaction channel concentrically encompasses at least an inner multiple helix of an inner reaction channel and wherein the inflow side of each reactant conduit is directly or indirectly connected to each multiple helix.

[0027] The connection of a multiple helix to the primary distributor channels is in particular effected via the mixing section and a secondary distributor channel. Even if in the present case the secondary distributor channel and the collection channel are described and accounted for as separate from the multiple helix the multiple helix may comprise a secondary distributor channel at the inflow side and / or analogously a collection channel at the outflow side. In a further embodiment of the reactor, it may be advantageous when in the case of two or more reaction channels / multiple helices the inflow side of each reaction channel configured as a multiple helix is connected to a dedicated secondary distributor channel and / or mixing section.

[0028] In a further embodiment of the reactor, it may be advantageous when at least one further, secondary distributor channel and / or an inlet into each helix channel is arranged downstream of the at least one inflow-side secondary distributor channel in the direction of the longitudinal axis.

[0029] A further, secondary distributor channel combines the helix channels of a reaction channel before complete conversion and a reactant, for example the reactant 1 already introduced at the outset, and / or a catalyst may be introduced in a defined volume flow. This makes it possible for example in the case of incomplete conversion of reactant 2 to achieve complete conversion through postintroduction of reactant 1 . Downstream of the further, secondary distributor channel the altered reaction mixture is again transmitted in helix channels.

[0030] In a further embodiment of the reactor, it may be advantageous when the outflow-side collection channel or an outflow-side discharging chamber is connected to an outlet throttle and / or outlet nozzle and / or comprises said throttle and / or nozzle.

[0031] Such an arrangement makes it possible to achieve a pressure increase and pressure uniformization in the reaction channels of the multiple helix in the reactor. When the outlet throttle or outlet nozzle is controllable this makes it possible to effect outlet-side control of the pressure.

[0032] It is altogether advantageous when the collection channels are arranged in stages in the manner of a cascade. This may comprise the helix channels of each individual multiple helix opening into respective first collection channels. These first collection channels are connected to one another, for example via annular or conical sections or further collection channels. The terminal connecting channel in the flow direction comprises a conduit connection to a discharging chamber and / or to the product conduit.

[0033] In a further embodiment of the reactor, it may be advantageous when the smallest width (B) of the cross-sectional area (A) of the helix channel is 0.8 mm to 3 mm, ideally 0.8 mm to 2 mm. The helix channels are advantageously dimensioned such that a laminar flow is formed in their interior.

[0034] In the case of a circular cross section the diameter is advantageously 1 .1 times to 1 .5 times the aforementioned width (B).

[0035] In principle, the cross section / the cross-sectional area of a helix channel may have any geometric shape, wherein particularly advantageous shapes for heat exchange include stretched, slot-like shapes, such as oval, elliptical or rectangular cross-sectional areas. "Rectangular" is to be understood as also encompassing a shape which is substantially rectangular and where for example the corners are rounded or the short side is a sole radius or else shapes such as a parallelogram or a trapezium.

[0036] Here, the shortest path for each molecule to the first heat exchanging wall should be 1 of the aforementioned values.

[0037] It is advantageous when the flow cross sections of the helix channels of a reaction channel are dimensioned such that the flow rate of the reaction mixture in all helix channels of all reaction channels is identical or largely identical. In this way the average residence time of the substances / the individual molecules in the reaction section of the reactor is identical or largely identical so that all reaction sectors in the interior of the reactor afford a product of identical or at least very comparable quality.

[0038] In a further embodiment of the reactor, it may be advantageous when the cross-sectional area (A) in the helix channel has an elliptical, oval or at least approximately rectangular basic structure, wherein advantageously the ratio of the smallest extent (width B) to the largest extent (height H) of the cross-sectional area is not less than 0.5, ideally in the range from 0.2 to 0.06.

[0039] Ideally in a vertical section the largest longitudinal extent of the cross-sectional area A is aligned parallel to the longitudinal axis (height H) and the smallest longitudinal extent (width B) is oriented in the radial direction.

[0040] In other words, the helix channels of a reaction channel are in the form of flat channels which are arranged in a spiral at a fixed distance around the central longitudinal axis, wherein the long sides thereof are aligned in the direction of the longitudinal axis and in alignment with one another so that the helix channels span a theoretical (enveloping) cylindrical annulus or annular slot. The long sides of the helix channels are arranged parallel or substantially parallel to the sides of the aforementioned theoretical annular slot.

[0041] In a further embodiment of the reactor, it may be advantageous when at least one sensor holder for accommodating and / or securing a sensor is provided, wherein the sensor holder comprises a sensor pier, which is connected at one end to a helix channel in the interior, and wherein the sensor pier passes through the interior and through the reactor wall of the main body. Outside the main body, a sensor accommodated and secured in this way is connectable in a data-conducting manner to a data receiver and / or a control unit. The connection of the sensor pier to a channel in the interior of the reactor represents a wall, in particular a channel wall, which is the measurement site for the free, measurement end of the sensor.

[0042] The sensor holder and in particular also the sensor pier are advantageously made of the same main material as the reactor. The sensor pier is not to be understood in a limiting sense and means a closed duct of a principally removable and replaceable sensor, for example a rod-shaped temperature sensor, vibration sensor or flow sensor. The sensor pier passes through the interior of the reactor at an angle and traverses internal channels and wall sections made of solid material until it reaches the measurement site. A sensor pier can therefore comprise or be formed from tube- or shell-like sections for bridging internal cavities and opening sections for penetrating wall sections.

[0043] In a further embodiment of the reactor, it may be advantageous when every reaction channel or at least one helix channel of each reaction channel has a sensor pier of a sensor holder leading to it, in particular a plurality of sensor piers are arranged in the direction of the longitudinal axis. The advantage of this arrangement is that it allows optimal detection of reaction progress in the flow direction and influencing of reaction progress by open- and closed-loop control.

[0044] In a further embodiment of the reactor, it may be advantageous when each individual helix channel has at least one sensor pier leading to it, in particular a helix channel of every reaction channel has at least two sensor piers leading to it. It is preferable when every helix channel is connected to at least two sensor piers and sensor holders via a respective measurement site.

[0045] There is altogether also a need to operate this reactor as energy efficiently as possible. In a further embodiment of the reactor, it may thus be advantageous when the interior comprises at least two separate heat exchange spaces or channels (HES) and / or groups of heat exchange channels which are fluidically and spatially separated from one another by at least one separating element and / or as a section of the interior, wherein each HES / channel has at least one feed conduit and one discharge conduit, wherein each HES / channel is operable with a different heat transfer medium and / or at its own temperature level.

[0046] The great advantage of such dual temperature operation are improved heat exchange and lower energy consumption. The first strongly exothermic reaction sector may for example be operated with a higher volume flow and / or at a lower temperature level, in particular be operated at a lower temperature level on the inflow side, via the first of two HES / channels. The subsequent reaction sector which is only very slightly exothermic, if at all, may be performed at a lower volume flow, at a higher temperature level and / or with a more economic heat transfer medium using the second HES / channel. Such a design and operating mode with at least two separate heat exchange circuits are more economic and sustainable in the long term.

[0047] This further embodiment of the reactor may advantageously be improved in that the separating element comprises an insulation layer and / or is at least partially manufactured from a thermally insulating material. The insulating layers may be for example an internal insulating layer and / or may be at least partially formed from a metal foam, a fibre material or from a comparable material or material mixture for example.

[0048] All apparatuses which are to be used to perform strongly exothermic reactions or in which explosive substances are transported or conducted shall advantageously have redundant risk protection. It is particularly advantageous when in a further embodiment of the reactor the main body has a protective housing arranged around it. The protective housing may especially be configured as a bursting, fragmentation and / or fire protection element, especially according to DIN EN 1127-x.

[0049] This further embodiment of the reactor having a protective housing can advantageously be improved in that the protective housing comprises an extraction, a filter unit and / or an absorption unit and / or is connectable thereto.

[0050] A filter or absorption unit especially comprises a nonflammable filter or absorption medium which is made for example of zeolite, bentonite, a metal foam or a comparable material.

[0051] In a further embodiment of the reactor, it may be advantageous when downstream of the at least one inflow-side distributor channel in the direction of the longitudinal axis at least one helix channel of a first reaction channel is combined with at least one helix channel of another reaction channel, especially each of the helix channels of the first reaction channel are combined with a respective different helix channel of another reaction channel.

[0052] In other words, two multiple helices become only one multiple helix. This design has the advantage that a reaction sector with only low exothermic reaction characteristics benefits from simplified construction and thus easier manufacturing of the reactor. Furthermore, by continuing the reaction sector in helix channels, especially with accompanying heat exchange channels, the compact, small design of the entire reactor is retained.

[0053] Advantageously a respective helix channel from each reaction channel / from each multiple helix is combined and continued downstream in / as a single (secondary) helix channel.

[0054] The improved mixing also improves the consumption of the reactants and the product quality. Based on the total reaction duration / the residence time of a molecule in the reaction sector, the reaction sector in the secondary multiple helix corresponds to at least 50% of the total reaction duration, in particular at least 75% of the total reaction duration.

[0055] In a further embodiment of the reactor, it may be advantageous when downstream of the at least one inflow-side distributor channel in the direction of the longitudinal axis the helix channels of at least two reaction channels are passed via a collection unit into a common reaction tube, in particular a common reaction tube dimensioned such that the residence time of the reaction mixture

[0056] - corresponds to at least 50% of the total reaction duration, in particular

[0057] - corresponds to at least 75% of the total reaction duration.

[0058] In a departure from the aforementioned reactor design with a secondary multiple helix as the secondary multiple helix / secondary reaction sector the reaction tube is in particular a substantially straight tube.

[0059] In the present case a reaction mixture is to be understood as meaning a mixture of reactants, intermediates and / or product which in the flow direction (F) changes in composition and in the concentration of the individual mixture proportions as a result of ongoing reaction.

[0060] The collection unit, which represents the transition from the reactor to the reaction tube, may be identical to the aforementioned collection channel. The reactor is therefore shorter in the longitudinal direction and therefore easier and more economic to manufacture. The common reaction tube is advantageously connected to a heat exchange circuit and suitably temperature- controlled, wherein this heat exchange circuit may be independent of that of the reactor and / or structurally separate.

[0061] In a further embodiment of the reactor, it may be provided that two reactors are arranged in series, in particular that the collection section of the first reactor in the flow direction represents the distributor section of the second reactor and / or the discharging section of the first reactor forms the introduction section of the second, subsequent reactor.

[0062] Such an arrangement is advantageous for example in linked syntheses of in each case highly exergonic reactions, such as the oxidation of ethene to acetaldehyde in a first step and first reactor and the oxidation of acetaldehyde to acetic acid in a further step and second reactor. A feeding of further reactants and / or catalysts upstream of or for the second reactor may be provided for.

[0063] The invention further comprises a plant for performing a synthesis process for producing products from at least two reactants with at least one reactor, wherein the at least one reactor is configured according to one of the variants and / or embodiments described above.

[0064] A further improved embodiment comprises at least two reactors configured according to any of the variants and / or embodiments recited herein and arranged in parallel.

[0065] The at least two parallel reactors may be connected at the outflow side to a common product conduit. Similarly, the at least two parallel reactors may be connected at the inflow side to a common reactant conduit. In one embodiment of the plant, it may be advantageous when the at least two reactors are connected at the outflow side to at least one common reaction tube, in particular to a common reaction tube which is dimensioned such that the residence time of the reaction mixture in the reaction tube

[0066] - corresponds to at least 50% of the total reaction duration, in particular

[0067] - corresponds to at least 75% of the total reaction duration.

[0068] The reaction tube may also be a tubular reactor or be named as such. The common reaction tube is advantageously connected to a heat exchanger circuit, in particular temperature-controlled via a dedicated heat exchanger circuit and / or heat exchanger. In a further advantageous embodiment of the reaction tube this comprises in a central position at least one elongated heat exchange element which extends over a partial length in the direction of the longitudinal axis of the reaction tube so that the reaction space in the reaction tube has the shape of an annular slot or annular channel. In addition to the internal heat exchange element the reaction tube may have a jacket heat exchange element.

[0069] Similarly to the aforementioned reactor a reaction tube may comprise at least one sensor holder for a sensor, in particular for two or more sensors which are arranged in the longitudinal direction.

[0070] In a further embodiment of the plant it may be advantageous when downstream of the at least one reactor the product conduit is connected to a degassing unit comprising: the product conduit as a feed conduit, a first discharge conduit for the product and / or the substance mixture 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 not more than 2 bar, preferably not more than 1 bar, especially a vacuum of up to 0.5 bar.

[0071] At least one further separation unit for separating substances from the product and / or purifying the product may advantageously be provided downstream of the degassing unit.

[0072] The invention further comprises a production process for a reactor for the synthesis of a product, wherein the reactor is configured according to any of the variants or embodiments recited herein and wherein the reactor is manufactured by means of

[0073] - a computer-implemented process (CIP) or partial process, and

[0074] - an additive manufacturing process (AMP) via an additive manufacturing apparatus (AMA).

[0075] The CIP advantageously comprises the following steps: provision of primary data from a database and / or via an input unit (HMI) for a process simulation program (CSD), wherein the primary data may especially be process data, flow data, substance and media data, reaction data; single- or multi-step simulation of the reaction using the process simulation program (CSD); generation of design data via the process simulation program (CSD); provision and receipt of executable control data for implementation of the design data for the AMA, wherein the executable control data are at least partially generated in the process simulation program (CSD) and / or the AMP or a processor of the AMA and performance of the AMP

[0076] In this case, "providing" data is always also to be understood as meaning that said data is at least temporarily stored on a nonvolatile storage medium and in the subsequent process step is retrieved by the respective apparatus / the accompanying processor unit and executed with a suitable (software) program. The term "storage medium" is not to be understood in a limited sense and comprises internal and external storage media and all types of wired-connection or wirelessconnection storage media. In addition, "providing for" is also to be understood as meaning that the unit recited in the particular case acquires the provided data or data packet and uses it as intended with an executable software program using at least one processor.

[0077] In a further embodiment of the production process, it may be provided that the AMP is a powder bed-based melting process and / or a process with directed energy deposition, in particular a laser-, electron beam- or plasma-induced, powder bed-based melting process. Alternatively or in addition, it may be provided that the AMA is configured for performing such an AMP. The AMP can also be referred to as metallic 3D printing and / or represents such 3D printing.

[0078] In a further embodiment of the production process, it may be advantageous when the computer- implemented process or partial process comprises the following steps: a) provision of process data and design parameters for CAD software, b) determination of design data via the CAD software or a CAD model, c) provision of control data for an additive manufacturing apparatus, d) production of the reactor by the AMA.

[0079] The process data are especially material data and reaction-technical and thermodynamic data and dependencies. Step b) may also comprise a single- or multi-step simulation after repetition of step a). The determination of the design data and / or of the CAD model is advantageously carried out with at least one determination of strength, in particular via a calculation and / or simulation step according to FEM (finite element method).

[0080] The synthesis of the reaction is advantageously simulated, optionally simulated multiple times, using simulation software, such as CFD (computational fluid dynamics). These simulation data, which may comprise process data, reaction data, thermodynamic data and other data, are subsequently at least partially provided to the CAD software for design of the reactor and evaluated / employed by the CAD software. This comprises in particular the creation of a CAD model of the reactor as a data set. The CAD model or data set is provided to a display and / or output unit, for example a monitor, provided in at least one known display and / or output format, for example provided on a storage medium and / or the output unit as a .t_x file for example. It is moreover advantageous when the CAD software is provided with the number, type and / or measurement location of the sensors / the accompanying sensor holders as data and / or when the CAD model comprises the number, type and / or measurement locations of the sensors. The obtained CAD model is ideally made available to a control unit with calculation software or retrieved from a data storage means by the calculation software, wherein the calculation software is configured to produce calculation steps to verify the strength of the reactor according to the respective CAD model by means of FEM (finite element method). Advantageously, the steps of the CFD simulation, CAD modelling and / or FEM calculation are iteratively repeated one or more times until a desired and / or legally required design (CAD model), in particular required strength of the reactor, is achieved. In the present case "CAD model" as the data set is not to be understood in a limiting sense and comprises not only the complete CAD model but also all data sets, reports and any data formats that have been derived at least in part from the CAD model by the CAD software and / or determined on the basis of the CAD model.

[0081] The invention further comprises a storage medium comprising at least one executable program code

[0082] - for performing the production process according to at least one of the variants and embodiments referred to herein and / or

[0083] - for controlling an AMA for performing the production process according to at least one of the variants and embodiments recited herein.

[0084] The storage medium may be a portable, non-volatile storage means, such as a CD, DVD, USB stick, etc. or be part of a computer or processing unit, such as a computer, a server, a processor unit, a microprocessor unit. Furthermore, the associated data connection and / or the interface is not limited and may be connected by wire or connected wirelessly.

[0085] In one embodiment it may be advantageous when the storage medium is a storage medium which is integrated in the AMA or connected or connectable to the AMA in a data-conducting manner.

[0086] The advantages and aspects recited herein for the reactor altogether apply to the plant in identical or analogous fashion and vice versa. The advantages and aspects of the production or synthesis process recited herein shall also apply to the reactor and / or the plant unless something specific or limiting is elaborated.

[0087] The invention further comprises a synthesis process for a product by a (chemical) reaction which comprises the following steps: a) provision of at least one reactor; b) provision of a first liquid reactant; c) provision of a second liquid reactant, wherein the second reactant may be a substrate which comprises or contains a catalyst; d) provision of a liquid heat transfer medium; e) continuous supplying of the reactor with first reactant, second reactant and heat transfer medium; f) continuous mixing of the first liquid reactant with the second liquid reactant in a mixing section of the reactor to obtain a liquid reaction mixture; g) continuous conversion by reaction of the reactants 1 with the reactant 2, in particular also with the reaction products, downstream of the mixing section and inside the reactor to afford a liquid product or product mixture, and wherein at least a portion of the reaction heat formed during the reaction is transferred from the reaction mixture and / or the product mixture to the heat transfer medium by means of the reactor; h) continuous withdrawal of the product mixture from the reactor; i) continuous withdrawal of the heat transfer medium from the reactor; wherein the reactor is configured according to one of the variants and / or embodiments recited herein and / or the process is performed with / in a plant according to one of the variants and embodiments recited herein.

[0088] It is advantageous when the continuous supplying of the reactor with first reactant, second reactant and heat transfer medium according to step e) is preceded by commencement of the flow of the heat transfer medium followed by first supplying of the reactor with the second or both reactants.

[0089] In the current case the terms “conversion”, “synthesis (process)” or “(chemical) reaction” are used substantially synonymously in the absence of any specific indications. Furthermore, the term "reaction" is generally to be understood as meaning the chemical reaction that produces the respective desired (main) product. The reactants are especially pressure-liquefied substances which are gaseous or vaporous under atmospheric conditions.

[0090] In one variant of the synthesis process it may be advantageous when step e) is preceded by provision of a third reactant (reactant 3) which comprises at least one catalyst or represents a catalyst and wherein the reactants are mixed consecutively, simultaneously or largely simultaneously in step f). In this case the reactor comprises a corresponding third reactant conduit and especially analogous distributor channels, flow splitters etc. as described for the first and / or the second reactant and the accompanying reactant conduits.

[0091] In one variant of the synthesis process it may further be advantageous when the (process) pressure (p1) of the reactants is in the range from 10 bar to 100 bar, advantageously in the range from 20 bar to 80 bar, ideally in the range from 35 bar to 65 bar. In one variant of the synthesis process it may further be advantageous when said process comprises a strongly exothermic reaction, in particular a reaction where not less than 70 kJ are released per mole of reactant 1 , preferably not less than 80 kJ are released per mole of reactant 1 , in particular between 85 kJ and 150 kJ are released per mole of reactant.

[0092] In one variant of the synthesis process it may further be advantageous when the reaction in the reactor forms no volatile byproducts, in particular no volatile byproducts that require continuous removal, in particular that require continuous distillative removal. The reaction especially does not comprise continuous withdrawal and discharging of byproducts for example in a vapour phase for maintenance of the reaction.

[0093] In one variant of the synthesis process it may further be advantageous when the reaction is selected from the group of the following reactions: a. (poly)addition, b. polymerization of monomers with carbon double bonds (C=C double bonds), c. oxidation of organic compounds, d. Beckmann rearrangement for synthesis of carboxamides e. polymerization of butadiene and production of polybutadiene. f. .

[0094] In one variant of this synthesis process it may further be advantageous when the (poly)addition is an alkoxylation and the polymerizations of monomers with carbon double bonds (C=C double bonds) is in particular a free-radical polymerization selected from the group of the following reactions: of acrylates, methacrylates, styrene, maleic anhydride and vinyl compounds.

[0095] In one variant of the synthesis process it may further be advantageous when the reaction is an alkoxylation reaction for producing alkoxylates, wherein a) the first liquid reactant is an alkylene oxide selected from the group of: ethylene oxide, (EO), propylene oxide (PO), 1 -butylene oxide (BO), styrene oxide (SO); b) the second liquid reactant is a substrate / a compound selected from the group of: alcohols, fatty alcohols, phenol, alkyl phenols, amines, carboxylic acids and esters thereof, mercaptans and imidazolines.

[0096] In one variant of the synthesis process it may further be advantageous when the catalyst is a multimetal cyanide complex catalyst or alkali metal or alkaline earth metal hydroxide, in particular sodium hydroxide, potassium hydroxide and caesium hydroxide, or a basic catalyst, for example alkali metal alkoxides, in particular sodium methoxide and potassium methoxide, or a tertiary amine. In other variants of the synthesis process said process may be configured as follows: a. the (poly)additions are selected from the group of the following reactions:

[0097] - alkoxylation, ethylene cyanohydrin from HCN and ethylene oxide,

[0098] - (meth)acrylic esters from (meth)acrylic acid with alcohols or amines,

[0099] - urethanes from isocyanates with alcohols or amines,

[0100] - addition reaction of carboxylic acids or carboxylates onto epoxides, for example bisphenol glycidyl ether addition where additions onto bisphenol glycidyl ether are effected ,

[0101] - hydrogenation reactions,

[0102] - hydrosilylation,

[0103] - hydroformylation; b. the polymerizations of monomers having carbon double bonds (C=C double bonds), such as especially free-radical polymerization, wherein the polymerizations are selected from the group of the following reactions: of acrylates, methacrylates, styrene and vinyl compounds, polymerization of butadiene and production of polybutadiene; c. the oxidations are selected from the group of the following reactions:

[0104] - epoxidation of olefins, for example with oxygen or peroxides, especially with hydrogen peroxide according to the HPPO process, or else

[0105] - oxidation of isobutane to tertiary-butyl hydroperoxide,

[0106] - oxidation of methanol to formaldehyde,

[0107] - oxidation of propene to acrolein,

[0108] - oxidation of acrolein to acrylic acid,

[0109] - oxidation of ethene to acetaldehyde,

[0110] - oxidation of acetaldehyde to acetic acid,

[0111] - direct oxidation of ethene to acetic acid,

[0112] - oxidation of cyclohexane to adipic acid,

[0113] - reactions likewise to be understood in the context of an oxidation, such as for example

[0114] - nitrations

[0115] - halogenations, wherein the halogenations may be chlorinations or sulfochlorinations for example.

[0116] In one variant of the synthesis process it may further be advantageous when the oxidation reaction is a Baeyer-Villiger oxidation. This comprises an oxidation of ketones to carboxylic esters with peracids such as peroxybenzoic acid, 3-chloroperoxybenzoic acid (MCPBA), peroxyacetic acid or trifluoroperoxyacetic acid.

[0117] In one variant of the synthesis process it may further be advantageous when the oxidation reaction is an Andrussov process. This comprises an ammoxidation of methane at 1000°C over Pt / Rh catalysts to produce hydrocyanic acid. CH4 + NH3 + 1 .5 O2 —> HCN + 3 H2O. This is accompanied by an energy release of 474 kJ / mol.

[0118] The invention is demonstrated in figures with the aid of exemplary embodiments and described by way of example. In the drawings

[0119] Fig. 1 shows two partial views of the reactor in a first embodiment in plan view,

[0120] Fig. 2 shows the whole of the reactor according to figure 1 in a vertical sectional view,

[0121] Fig. 3 shows the reactor in the sectional view according to figure 1 as an enlarged partial view of the upper section (distribution section),

[0122] Fig. 4 shows the reactor in a horizontal sectional view in the upper section,

[0123] Fig. 5 shows the reactor in a horizontal sectional view at the height of the mixing section,

[0124] Fig. 6 shows the reactor in the sectional view according to figure 1 as an enlarged partial view of the central section (reaction section),

[0125] Fig. 7 shows the reactor in a horizontal sectional view at the height of the central section,

[0126] Fig. 8 shows the reactor in the sectional view according to figure 1 as an enlarged partial view of the lower section (collection section),

[0127] Fig. 9 shows the reactor in a horizontal sectional view at the height of the lower section and Fig. 10 shows the plant with the reactor in a second embodiment.

[0128] Figure 1 shows in perspective lateral plan view a partial view I of the reactor 100 in one embodiment, said reactor comprising a main body 102 elongated in the direction of the longitudinal axis 104 and having an inflow side 106 and an outflow side 108. In terms of geometric shape, aside from feed and discharge conduits, the main body 102 substantially comprises a conical section at the inflow side and the outflow side and a substantially cylindrical middle section.

[0129] From a functional perspective the reactor 100 comprises a distribution section 134, a mixing section 127, a reaction section 135 and a collection section 136. An introduction section 124 is arranged above the distribution section 134 on the inflow side and a discharging section 138 is connected below the collection section 136 on the outflow side. The reactor 100 comprises a first reactant conduit 119 for a first reactant, a second reactant conduit 120 for a second reactant, a feed conduit 140 for a HTM, a product conduit 130 for discharging a product or a substrate containing the product, a discharge conduit 142 for the heat transfer medium. The functions and the channel and conduit routing of the individual sections will be more particularly described below in conjunction with the partial view II. and the following figures.

[0130] The reactor 100 further comprises a multiplicity of sensor holders 152. A sensor holder 152 is configured here for accommodating a sensor 150 which may be introduced or held in the sensor pier 154 or the sensor channel by the accompanying sensor or measurement end. Below, a sensor pier 154 is generally to be understood as meaning a guide and holder which is arranged on the outside of the main body 102 and is configured as a substantially hollow guide tube with an appropriate securing and / or clamping apparatus. In the interior 110 of the reactor 100 not shown in figure 1 the sensor pier 154 has sections which are configured as an opening or cutout if a solid material is penetrated in the direction of the sensor axis 156 and are configured as a guide tube if an inner cavity or an inner channel is bridged until the defined measurement site 158 in the interior 110 of the reactor 100 is reached as the defined end of the sensor pier 154. In the present case reference is consistently made to a “sensor pier” even if, as described above, this is not configured as a continuous “pier”. The sensor axis 156 corresponds to the axis of the sensor holder 152 / of the sensor pier 154 and therefore “sensor axis” is in the present case to be interpreted correspondingly broadly.

[0131] This exemplary embodiment shows, by way of example, two sensors 150 which are each held in a sensor holder 152, wherein the sensor or measurement ends (not shown) of the respective sensors 150 are inserted up to the respective measurement site 158. Altogether four groups of three sensor holders 152 in each case are arranged on the circumference of reactor 100. The measurement sites 158 of the sensors 150 are arranged in the interior 110 in each case immediately adjacent to a helix channel 210, 212 as is shown in detail hereinbelow especially in figure 6 and figure 8. All sensors 150 are connected to a control unit 600 via the data conduits shown as dot-dashed lines. The control unit 600 serves to receive the measured signals of the sensors 150 and may comprise electronic components, in particular microelectronic components, to process, store and / or evaluate the measured signals, in particular may comprise components for converting analogue measured values into digital data.

[0132] In the example shown in each case three sensors 150 arranged in alignment with one another form a respective sensor group which monitor inner channels at three height levels of the longitudinal axis 104. Thus, the measurement sites 158 of the first sensor group are assigned to different height levels of the outer reaction channel 200 (see partial view IL), the measurement sites 158 of the second sensor group are assigned to different height levels of the inner reaction channel 202, the measurement sites 158 of the third sensor group are assigned to different height levels of the outer heat exchange channel 144 and analogously the measurement sites 158 of the fourth sensor group are assigned to an inner heat exchange channel 145, 146 or 147 (see especially figure 4).

[0133] In the present exemplary embodiment one sensor group monitors two of the inner helix channels 210 of the outer reaction channel 200 at different height levels. A first sensor group is arranged such that it monitors the first helix channel 210 at an upper and a lower position and monitors the third helix channel 210 at a central position. A second sensor group is arranged such that the third helix channel 210 is monitored at an upper and a lower position and the first helix channel 210 is monitored at a central position. The third and fourth sensor group is arranged such that the helix channels 212 of the inner reaction channel 202 are monitored in analogous fashion, wherein for design reasons three of the four helix channels 212 or four of the four helix channels are monitored at different height levels. In the present case the third sensor group monitors the first helix channel 212 in the upper and the lower position, wherein the second helix channel 212 is monitored in the central position. The fourth sensor group monitors the upper and the lower position of the third helix channel 212 and the fourth helix channel 212 is monitored in the central position.

[0134] Carrier elements 107 by which the reactor 100 can be mechanically secured to a holder and carrier unit (not shown) are arranged on the main body 102 at the height of the cylindrical reaction section 135. Any customary temporary or permanent securing means may be provided.

[0135] The partial view II. shows the same reactor 100 according to partial view I. but only the channels of the two reactants, of the reaction mixture and of the product are shown as a perspective plan view. In other words partial view II shows a liquid surface as a negative of the associated channel and all wall structures are removed in this representation. Furthermore, all conduits and internal channels for the heat transfer medium are not shown in the partial view II., i.e. the feed conduit 140, the discharge conduit 142 and all associated channels, such as for example the inner heat exchange channels 144, 145 and 146, and the helix- or spiral-shaped heat exchange channels 147.

[0136] In the present case and following the figures reference is made to “top”, “laterally”, “beside” and “bottom” or analogously “above”, “below”, “height level” or “height”. This type of description is only for ease of language and follows the example shown for the reactor 100 which is shown in the vertical orientation and in the example is traversed from top to bottom and has the reactant conduits 119, 120 arranged at the top and the product conduit 130 arranged at the bottom. In the present case the aforementioned type of description also correlates with the flow direction of the media in the reactor 100 and, in the absence of any specific indications or indications to the contrary, is synonymous for the flow direction of the respective media.

[0137] However, this is not to be understood as limiting in the absence of any specific indications because the reactor 100 can fundamentally assume any orientation, with the result that the longitudinal axis 104 may also be oriented horizontally or at an angle to the vertical gravitational direction, thus analogously altering the other assignments of the elements, components and orientations.

[0138] Routed in the introduction section 124 are the two reactant conduits 119, 120 which, outside the main body 102, may comprise suitable connection elements (not shown), such as flanges, screw threads or other elements. In the distribution section 134 the reactant conduits 119, 120 comprise flow splitters 122 and flow spreaders 123. In the example shown at least one flow splitter 122 is arranged upstream of the flow spreaders 123 in the flow direction F in the respective reactant conduit 119, 120, with the result that the respective reactant conduit 119, 120 is split into at least two, presently four, conduit branches which lead to subsequent distributor channels 112, 114. The flow spreaders 123 form the transition / the introductory channel section for introduction of the respective reactant into the associated distributor channel 112, 114.

[0139] In the exemplary embodiment shown the (primary) distributor channels 112, 114 are four annular channels arranged concentrically to one another as is more particularly described especially in connection with figures 3 and 4. Arranged below the distributor channels 112, 114 and as a transition is the mixing section 127 by means of which in each case two distributor channels 112, 114 of in each case one of the reactants are in communication and open into two secondary distributor channels 129.

[0140] The two secondary distributor channels 129 each have a reaction channel 200, 202 connected to them. The reaction channels 200, 202 are each configured as a multiple helix which each comprise four helix channels 210, 212. In other words the reaction mixture present in the secondary distributor channel 129 is distributed over the four helix channels 210 of the reaction channel 200 and discharged. In the case of strongly exothermic reactions, for example an alkoxylation, the reaction commences immediately after contact of the reactants in the secondary distributor channel 129 so that the secondary distributor channel 129 is already assigned to the reaction section 135 which has an associated cooling demand.

[0141] The mixing section 127 is determined by the location of the transition and combination of the respective reactants to produce the reaction mixture, wherein the different reactants also continue to undergo especially fluid-mechanical mixing in the secondary distributor channel 129. The mixing section 127 is the transition from the distribution section 134 to the reaction section 135 of the reactor 100 and in figure 1 is shown overlapping with the two recited sections and in figures 2, 3 and 6 is shown delimited by the curly bracket. This does not represent different embodiments but rather shows the fluid transition of the distribution section 134 to the reaction section 135 in the region of the mixing section 127.

[0142] A multiple helix is in the present case to be understood as meaning a channel structure in which two or more channels are configured in a spiral shape, largely parallel to one another and spaced apart from one another in the vertical direction. The helix channels of a multiple helix are connected to a common secondary distributor chamber 129.

[0143] In an embodiment that is not shown the secondary distributor chamber is a ring section or comprises two or more ring sections, wherein at least two helix channels are connected to one ring section. All helix channels of a secondary distributor chamber configured as a ring section or all ring sections of a secondary distributor chamber form a common reaction channel. As shown in partial representation II of figure 1 , the outer reaction channel 200 configured as a multiple helix encompasses an inner reaction channel 202 likewise configured as a multiple helix, with both reaction channels 200, 202 each comprising four helix channels 210, 212.

[0144] For the sake of clarity, the four helix channels 210, 212 are not separately provided with reference numerals, wherein viewed in the sectional plane in the circumferential direction the first helix channel 210, 212 is on the left-hand side and the third helix channel 210, 212 is on the right-hand side in the image plane and these channels are shown as an elongate hole-like opening surface.

[0145] The collection section 136 which comprises a plurality of collection channels 1 16, 117, 119 is connected to the reaction section 135. In the collection channels 1 16, 117, the respective helix channels 210, 212 are combined and introduced into a product conduit 130. In the example shown a collection unit 132 which also has the function of a mixing and calming chamber is arranged between the last collection channel 1 18 and the product conduit 130.

[0146] At the lower end of the main body 102 a cone structure comprising two or four openings 160 is shown. These openings 160 represent the regions in which the heat transfer medium-conducting helical heat exchange channels 147 are guided radially outward where they are introduced or transition into a common collection channel 148 (not shown) (figure 2, figure 9).

[0147] The multiplicity of different channels in the interior 110 of the reactor are apparent in the representation of figure 2. The reactor 100 corresponds to that of figure 1 in partial illustration I and so what follows is especially a description of the elements and functions that were not previously described together with figure 1. The central longitudinal axis 104 is in the sectional plane (x-z plane). In the introduction section 124 the reactant conduits 119, 120 proceed out of the sectional plane and are thus not shown in their entirety. Figure 2 especially shows individual sections of the reactor 100, the position of the sections A to D and the assignment to figures 3 to 10, which show the reactor 100 according to figure 2 in sections and in greater detail.

[0148] The representation of figure 3 shows the reactor 100 in the sectional representation (x-z plane) according to figure 2 as an enlarged partial view of the upper section which comprises the introduction section 124, the mixing section 127 and the distribution section 134. The reactant 1 flowing in via the first reactant conduit 119 is divided from the two annular distributor channels 112 via the inner channels, flow splitters 122 and flow spreaders 123. The reactant 2 flowing in via the second reactant conduit 120 is analogously introduced from above into the two annular distributor channels 1 14 via the partially shown inner channels, the flow splitters 122 and the flow spreaders 123. The introduction from above via the flow spreaders 123 is effected outside the sectional plane and is shown as dashed arrows. The four annular distributor channels 112, 114 are arranged concentrically and in pairs so that a distributor channel 112 conducting the reactant 1 is always arranged adjacent to a distributor channel 114 conducting the reactant 2. The pairs of in each case four distributor channels 112, 114 and the distributor channels 112, 114 as a whole are arranged concentrically relative to one another. The mixing section 127 is arranged below the distributor channels 112, 114. The mixing section 127 is substantially formed from a multiplicity of mixing channels 128 which form the lower outlet from the distributor channels 112, 114 and lead to the inlet in one of the two secondary annular distributor channels 129. The mixing channels 128 of a pair of two directly adjacent distributor channels 112, 114 are arranged such that they lead into a common secondary distributor channel 129 so that in the subsequent distributor channel 129 the two reactants 1 , 2 are mixed and the reaction commences.

[0149] In the example shown, a mixing channel 128 leads alternately in the circumferential direction from each distributor channel 112, 114 into the downstream secondary (common) distributor channel 129.

[0150] The two distributor channels 112, 114 containing the in each case unmixed reactant 1 , 2 may also be referred to as primary distributor channels 112, 114 since they are traversed first.

[0151] The central feed conduit 140 transitions via branches into inner heat exchange channels 143-147 which are configured as concentric annular heat exchange channels 144-146 and as helical or spiral-shaped heat exchange channels 147. In the region of the distribution section 134 the heat exchange channels 144-146 are configured as concentric annular channels analogously to the distributor channels 112, 114. In the reaction section 135 the heat exchange channels 147 are configured as helix channels (figure 5). The inner distribution comprises a plurality of transverse distribution channels 143, one of which is in the sectional plane shown. As shown in figure 3, the central feed conduit 140 for a heat transfer medium immediately branches into an outer annular heat exchange channel 144 and a transverse channel 143. The top of the transverse channel 143 is inter alia connected to a central annular heat exchange channel 145 and an inner heat exchange channel 146 and feeds these. A pair of annular distributor channels 112, 114 thus has a heat exchange channel 144-146 that is likewise annular arranged on either side of it. In other words, two distributor channels 112, 114 for in each case one reactant of the two reactants, which form an adjacent pair and which open into a common secondary distributor channel 129, have a common dividing wall and each have one wall in common with an adjacent heat exchange channel 144 - 146. The annular heat exchange channels 144-146 and the distributor channels 112, 114 / the pairs thereof encompass one another concentrically.

[0152] In the example shown the heat exchange channel 144 is arranged radially outwardly, followed in the radial direction towards the longitudinal axis 104 by the outer pair of two distributor channels 112, 114, the central heat exchange channel 145, which concentrically encompasses the inner pair of two distributor channels 112, 114, and the innermost annular heat exchange channel 146, concentrically encompassed by the inner pair of distributor channels 112, 114 and all other annular channels in this reactor section. A further particular advantage found is that the concentric arrangement of the annular slot -shaped distributor channels 112, 114 on the one hand and the also annular slot-shaped heat exchange channels 144, 145, 146 on the other hand brings about a heating and / or a temperature equalization of the fluids present therein already in the distribution section 134. In a test setup the reactants were supplied at a temperature of 15°C to 20°C and the HTM at a temperature of about 60°C. Already in distribution section 134 the HTM was cooled by about 20°C to 25°C and the reactants in the distributor channels 112, 114 were heated by a comparable value. This has the result that less energy is required for the thermal regeneration of the HTM and the temperature levelling avoids stresses in the reactor body. In other words it was demonstrated very generally for the reactor and (synthesis) processes performed therewith that it is advantageous when the HTM, here an oil, serves as a heating medium which heats the cooler reactants and thus accelerates the reaction / the start of the reaction upstream of the distribution section 134. Downstream of the distribution section 134 the substance mixture present there is hotter than the HTM which then serves as coolant.

[0153] Figure 3 further shows the inclined mixing channels 128 which are in the sectional plane and lead out of the bottom of the distributor channels 112, 114 into the respective common annular distributor channel 129.

[0154] Figure 4 shows the reactor 100 in a horizontal sectional representation (x-y plane) in the distribution section 134 - this corresponds to section A-A in figure 2. Arranged on the outside of the main body 102 are sensor holders 152 wherein four are shown completely in the plan view from above and four are additionally shown as a sectional surface. The sensor holders 152 are arranged in alignment with one another along routes parallel to the longitudinal axis 104. Also shown is a carrier element 107 in section and the lower discharge conduit 142 in plan view. As already explained in connection with figure 3, each pair of annular distributor channels 112, 114 has two likewise annular heat exchange channels 144-146 arranged adjacent to it. This results in the following sequence of concentric channels from outside to 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), innermost heat exchange channel 146.

[0155] In the representation of figure 5 the reactor 100 is shown in a horizontal sectional view (x-y plane) at the height of the mixing section 127, this corresponding to the section B-B in figure 2. On the outside of the main body 102, analogously to the representation of figure 4, eight sensor holders 152 are shown, wherein all six of the eight are also shown as a sectional plane. The sensor holders 152 are arranged in (vertical) alignment with one another along routes parallel to the longitudinal axis 104. Figure 5 further shows two secondary distributor channels 129, a multiplicity of mixing channels 128 and sensor piers 154 in the interior 110. Arranged in close proximity over the entire circumference on the inflow side of each secondary distributor channel 129 are mixing channels 128 which are the outlets of the (primary) distributor channels 112, 114 (not shown) arranged thereabove. The penetration of the outer heat exchange channel 144 by the sensor piers 154 is also shown in the plane of the image at the top left and bottom right and the penetration of the central heat exchange channel 145 by two further sensor piers 154, wherein the sensor piers 154 are especially configured as a guide channel or opening in the region of the central heat exchange channel 145. The sensor piers 154 thus form an integral mechanical structure in the interior 110 of the reactor 100.

[0156] Figure 6 shows the reactor 100 in the sectional view (x-z plane) according to figure 1 as an enlarged partial view of the central section (reaction section 135). Figure 6 comprises the mixing section 127, the reaction section 135 and an initial section of the collection section 136. Arranged in the reaction section 135 are an outer reaction channel 200 and an inner reaction channel 202 shown as dot-dashed lines and also heat exchange channels 147. The exemplary embodiment shown provides for three heat exchange channels 147 which are arranged in the following sequence from outside to inside in the radial direction: Heat exchange channel 147 (outer), reaction channel 200 (outer), heat exchange channel 147 (central), reaction channel 202 (inner), heat exchange channel 147 (inner). The reaction channels 200, 202 are configured as multiple helices. The multiple helix of the outer reaction channel 200 is formed from the helix channels 210 and the multiple helix of the inner reaction channel 212 is formed from the helix channels 212. The heat exchange channels 147 are at least partially formed as helix or spiral channels in the reaction section 135. Each reaction channel 200, 202 thus has a spiral heat exchange channel 147 adjacent to it on both sides and can thus be intensively cooled. At the inflow side the helix channels 210 of the outer reaction channel 200 are in fluid communication with the outer secondary distributor channel 129 and the helix channels 212 of the inner reaction channel 202 are in fluid communication with the inner secondary distributor channel 129 and are fed therefrom.

[0157] In the vertical sectional plane (x-z plane) the helix channels 210, 212 have a rectangular or virtually rectangular cross section with a height in the direction of the longitudinal axis 104 and a width radial or transverse to the longitudinal axis 104. In the exemplary embodiment shown the short sides are shown as radii and the long sides as substantially straight. The ratio of the width B to the height H for the surface A is under the desired process conditions selected such that a laminar flow is formed in the helix channel 210, 212. The Reynolds number Re is defined by the quotient

[0158] Re = p v L I p.

[0159] Here p = fluid density, v = flow velocity, L = characteristic length and p fluid viscosity. Re is advantageously not more than 9000. The area A in the sectional plane (x-z plane) is not identical to the channel cross-sectional area which is transverse to the main flow direction in the helix channel 210, 212, wherein if required this differentiation is to be undertaken analogously if the effect is correspondingly great, for example in the case of a very strong inclination of the helix channels 210, 212 so that the area A in the sectional plane cannot be equated to the flow cross section. If in doubt the flow cross section is to be used for configuration of the geometries. In the sectional plane (x-z plane) the spiral channels 147 have a largely rectangular, trapezoidal or parallelogram-shaped cross-sectional area at least on a partial length in the reaction section 135. It has proven advantageous when the cross-sectional area W1 of a central heat exchange channel 147 has at least 1 .3 times the surface area, in particular at least 2 to 5 times the surface area, compared to the cross-sectional area W2 of the innermost or outermost heat exchange channel 147.

[0160] The great advantage of the double and parallel winding of the heat exchange channel 147 and the reaction channel 200, 202 / the helix channels 210, 212 is that optimal cooling of the strongly exothermic reaction mixture is possible and hotspots are avoided at all times. This ensures that combustion of the reaction mixture is safely avoided and product quality is altogether improved and uniformized.

[0161] The reactor 100 is moreover optimally monitored via the multiple sensors 150 arranged on the flow path and controllable via the control unit 600. If an unfavourable temperature profile is detected on the reaction sector in a reaction channel 200, 202 or a sensor-monitored helix channel 210, 212, the reaction may be selectively influenced for example by reducing at least one reactant stream and / or the volume flow of the heat transfer medium.

[0162] In the representation of figure 7 the reactor 100 is shown in a horizontal sectional representation (x- y plane) at the height of the central reaction section 135 - this corresponds to the section C-C in figure 2. Figure 7 shows the four horizontal cross-sectional areas of the four outer helix channels 210 of the outer reaction channel 200 (figure 6), the four helix channels 212 of the inner reaction channel 202 (figure 6) and the four horizontal cross-sectional surfaces of each of the three spiral heat exchange channels 147. As is apparent from the sectional representations of figures 6 and 7, the heat exchange channel 147 is advantageously helical or spiral shaped and thus follows the helix structure of the helix channels 210, 212 in which the reaction is substantially carried out. However, the geometries and dimensions of the cross sections of the helix channels 210, 212 on the one hand and the spiral-shaped heat exchange channels 147 on the other hand differ from one another. The spiral-shaped heat exchange channels 147 are optimized for optimum heat dissipation. Figure 7 shows the measurement site 158 opposite two of the four inner helix channels 212 by way of example. To this end the sensor pier 154 is configured in the region of the solid material or the wall as a sensor guide or opening and bridges the central heat exchange channel 145 in the manner of a pier. The two measurement points 158 illustrated are arranged at a height in the reaction section 135 immediately adjacent to in each case one of the inner helix channels 212.

[0163] Figure 8 shows the lower end of the reaction section 135, the collection section 136 and the discharging section 138 of the reactor 100 in a vertical sectional representation (x-z plane) with the outflow side 108 of the reactor 100. In the flow direction F the reaction section 135 transitions into the collection section 136, to which the discharging section 138 is connected. In the collection section 136 the spiral heat exchange channels 147 and the annular or conical collecting channels 148 are cascaded together with conduits until all heat exchange channels 147 and collecting channels 148 are combined in the lowest collecting channel 149, thus combining the heat transfer medium into a single stream. The lowest connecting channel 149 is connected to the discharge conduit 142 by means of which the heat transfer medium is dischargeable from the interior 110 of the reactor 142.

[0164] In analogous fashion the helix channels 210, 212 are combined in cascading, terminal (product) collection channels 116, 118. In the depicted exemplary embodiment of figure 8, the groups of four helix channels 210, 212 of the respective reaction channels 200, 202 each open into a respective annular (product) collection channel 116 and said channels combine downstream into a common (product) collection space 118. This common (product) collection space 118 may in principle have any geometric shape and is advantageously annular, conical or a combination thereof. In analogous fashion the outer (product) collection channel 116 has an upper annular section which is parallel to the longitudinal axis 104 and has a lower conical section which opens into the common collection space 118 downstream.

[0165] Downstream of the lowest collection space 118 the exemplary embodiment of figure 8 further shows a discharging chamber 137 in the form of an internal chamber with a radially enlarged interior. This discharging chamber 137 provides an extended residence time for the product mixture, thus bringing about a uniformization and calming of the flow in terms of pressure. The discharging chamber 137 comprises a top region which conically widens in the flow direction F, a substantially cylindrical, elongate central region and a conically narrowing outflow or bottom section. The outflow side of the discharging chamber 137 is connected to the product conduit 130. Any required securing means or sections on the discharge conduit 142 and the product conduit 130 are not shown.

[0166] In figure 9 the reactor 100 is shown in a horizontal sectional representation at the height of the collection section 136 (x-y plane) - this corresponds to the D-D section in figure 2. In the sectional plane the channels appear as four concentric rings, wherein the two (product) collection channels 116 are arranged radially between the two collection channels 148 for the heat transfer medium. The sectional plane D-D is thus above the respective final collection channels 118, 149.

[0167] Example measurement

[0168] In an exemplary embodiment according to figures 1 to 9 the reactor 100 described above was used for an alkoxylation of propylene oxide C3H6O (reactant 1) and the chain initiator allyl C2H6O2 (reactant 2) with a liquid multimetal cyanide complex catalyst that had been admixed with reactant 2. The addition reaction may be described as follows:

[0169] The reactor and process conditions had the following data:

[0170] • Inner secondary distributor channel 129 in the form of an annular channel having an internal diameter of 11 .8 mm and an external diameter of 14.2 mm (channel width 2.4 mm) and a local flow rate of 4.21 e6kg / s.

[0171] • Outer secondary distributor channel 129 in the form of an annular channel having an internal diameter of 32.6 mm and an external diameter of 35 mm (channel width 2.4 mm) and a local flow rate of 8.25 e6kg / s, i.e. about double the flow rate of the inner distributor channel.

[0172] • The respective reaction channels 200, 202, each having four helix channels 210, 212, are connected to the two secondary distributor channels 129. The vertical cross-sectional area A (x-z plane) of the helix channels 210 of the inner reaction channel 202 had a height H in the z-direction of 3.29 mm and a width B of 1 .2 mm. For the outer reaction channel 200 the height H in the x-z plane was 5.3 mm and the width B was likewise 1 .2 mm.

[0173] The horizontal cross-sectional area A2 (x-y plane) of the helix channels 210 of the inner reaction channel 202 had a length L in the circumferential direction of 3.42 mm and a width B of 1 .2 mm. For the outer reaction channel 200 the horizontal cross-sectional area A2 had a length L in the circumferential direction of 12.072 mm and a width B of likewise 1 .2 mm.

[0174] • The flow rates in the respective four helix channels downstream of a secondary distributor channel 129 were % of the aforementioned value.

[0175] • The heat exchange medium employed was a heat exchanger oil.

[0176] • The reactor had altogether 12 sensor holders comprising 12 sensors, all of which were designed as temperature sensors and connected to a control and evaluation unit in a data- conducting manner.

[0177] • The reactor for the exemplary embodiment had the following dimensions:

[0178] - Total height 340 mm

[0179] - Diameter of pressure-bearing region 56 mm The experimental conditions are indicated in the following table:

[0180] Inflow kg I s g / min mol / min Temp. °C

[0181] (Feed)

[0182] Reactant 1

[0183] 1.0125e-05 0.6075 0.0138 25

[0184] (C3H6O)

[0185] Reactant 2

[0186] 2.375e-06 0.1425 0.00229 40

[0187] (C2H6O2)

[0188] Heat exchange medium 0.00495 297 - 90

[0189] In the region of the secondary distributor channel and the inflow of the subsequent helix channels 210, 212 the temperature in the reactor 100 attained up to 200.7°C. This is a non-critical hotspot with no adverse effect on product quality. The reactor 100 was operated continuously over a period under these conditions.

[0190] Having regard to the present flow rate of about 0.58 mm / s, the reaction mixture is subjected to this temperature of about 200°C in the region of the secondary distributor channel and in the inflow of a helix channel only over a distance of about 3 to 5 mm for a corresponding duration of about 5.16 sec. After about 10% to 15% of the length of the helix channel the temperature of the reaction mixture measured at the wall of the helix channel reached a value of less than 136°C. At the end of the helix channels a value of about 85°C to 92°C was continuously achieved. The geometry of the reactor 100 and in particular of the helix channels 210, 212 without any backmixing ensures that no fraction and no molecule was in fact subjected to the maximum process conditions for longer than mentioned above.

[0191] It was demonstrated that product quality was achieved or improved in every respect over the entire synthesis duration. The identical flow conditions and process conditions always defined in narrow parameter windows made it possible to achieve a higher product purity, in particular improved homogeneity and reduced turbidity.

[0192] The improved conversion with a lower propensity to form byproducts makes it possible to improve the ratio of the amounts (kg) of reactants to product compared to a stirred reactor.

[0193] Figure 10 shows, in highly schematic form, a plant 500 for producing products with the reactor 100, wherein the reactor 100 comprises a first reaction section configured analogously to the reactor 100 as described above and a plurality of reaction channels 200, 202 arranged concentrically to one another and configured as multiple helices.

[0194] Connected to the first reaction section 135 is a second reaction section 350 which is configured as a straight reaction tube 300. A separation unit 400 is arranged downstream of the reaction tube 300. In one embodiment of the process and the plants, the pressure prevailing in the reaction tube 300 is the same or substantially the same as that in the first reaction section 135 (not shown) of the reactor 100, wherein trace cooling or else trace heating may be provided. All reaction mixtures of the two or more helix channels 210, 212 are combined in the reaction tube 300. The already greatly calmed reaction which is now only slightly exothermic, if at all, is continued until the desired conversion. In the exemplary embodiment shown the flow path of a molecule in the main flow direction (flow direction F) within the reaction section 135 of the reactor 100 is in the range from 0.25 to 0.35 based on the total distance until the outflow 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 attainment of a conversion of at least 95% having regard to the desired product or the desired conversion. The reactor 100 and the reaction tube 300 are shown lying in an axis, wherein these may also have different alignments so that in an embodiment not shown in figure 10 the reactor 100 is vertically aligned and the reaction tube 300 is horizontally aligned, with suitable curved transitions between the two parts being provided.

[0195] A controllable throttle 302 which is connected to the control unit 600 in a data-conducting manner and controlled thereby is further provided in the product conduit 130.

[0196] The separation unit 400 comprises 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. The separation unit 400 effects a pressure reduction, which is not further specified, from the pressure p1 of about 30 to 40 bar in the reaction sections to the pressure p2 of about 1 bar, i.e. atmospheric pressure, in one or more steps. Volatile substances are thus separated in known fashion.

[0197] List of reference symbols

[0198] 100 Reactor

[0199] 102 Main body / housing

[0200] 104 Longitudinal axis (z-axis),

[0201] 106 Inflow side

[0202] 107 Carrier element

[0203] 108 Outflow side

[0204] 110 Interior

[0205] 112 Distributor channel

[0206] 114 Distributor channel

[0207] 116 Collection channel

[0208] 117 Collection channel

[0209] 118 Collection channel

[0210] 119 Reactant conduit

[0211] 120 Reactant conduit

[0212] 122 Flow splitter

[0213] 123 Flow spreader

[0214] 124 Introduction section

[0215] 127 Mixing section

[0216] 128 Mixing channel

[0217] 129 Distributor channel (secondary)

[0218] 130 Product conduit

[0219] 132 Collection unit

[0220] 134 Distribution section

[0221] 135 Reaction section

[0222] 136 Collection section

[0223] 137 Discharging chamber

[0224] 138 Discharging section

[0225] 140 Feed conduit

[0226] 142 Discharge conduit

[0227] 143 Transverse channel

[0228] 144 Heat exchange channel (outside) 145 Heat exchange channel (central)

[0229] 146 Heat exchange channel (inside)

[0230] 147 Heat exchange channel (helix)

[0231] 148 Collection channel

[0232] 149 Collection channel

[0233] 150 Sensor

[0234] 152 Sensor holder

[0235] 154 Sensor pier / channel

[0236] 156 Sensor axis

[0237] 158 Measurement site

[0238] 160 Opening

[0239] 200 Reaction channel, multiple helix

[0240] 202 Reaction channel, multiple helix

[0241] 210 Helix channel

[0242] 212 Helix channel

[0243] 300 Reaction tube

[0244] 302 Throttle

[0245] 350 Reaction section, second

[0246] 400 Separation unit

[0247] 402 Discharge conduit

[0248] 404 Gas discharge conduit

[0249] 500 Plant

[0250] 600 Control unit

[0251] A Cross-sectional area

[0252] F Flow direction

[0253] W Cross-sectional area, also W1 , W2

Claims

Claims1 . Reactor (100) for performing a synthesis process for producing products from at least two reactants comprising a. a main body having a longitudinal axis (104), an inflow side (106) and an outflow side (108); b. an interior (110); c. at least two reactant conduits (119, 120), each connected at the inflow side to at least one distributor channel (112, 116); d. at least one product conduit (130) connected at the outflow side to the at least one collection channel (116); e. at least one distribution section (134) comprising at least two distributor channels (112, 116) and at least one flow splitter (122); f. at least one mixing section (127) in which via mixing channels (128) at least two distributor channels (112, 116) are connected 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 comprising at least one collection channel (116); i. at least one inflow-side feed conduit (140) for a heat transfer medium into the interior (110) and at least one discharge conduit (142) for the heat transfer medium out of the interior (110), wherein- the heat transfer medium can flow around at least a partial length of the at least one reaction channel (200, 202) in the interior (110) and / or- at least one heat exchange channel in which the heat transfer medium can flow is provided, wherein this at least one subsection is arranged adjacent to the at least one reaction channel (200, 202) and wherein at least one heat exchange channel (147) and at least one reaction channel (200, 202) are separated from one another by a common channel wall, characterized in that the at least one reaction channel (200, 202) is a multiple helix which comprises two or more helix channels (210, 212), wherein at the inflow side each helix channel (210, 212) of a multiple helix 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 at the outflow side each helix channel (210, 212) of a multiple helix is connected to at least one collection channel (116).

2. Reactor according to Claim 1 , characterized in that said reactor comprises two or more reaction channels (200, 202) as a multiple helix, wherein an outer multiple helix of an outer reaction channel (200) concentrically encompasses at least an inner multiple helix of an inner reaction channel (202) and wherein each reactant conduit (119, 120) is directly or indirectly connected to each multiple helix.

3. Reactor according to Claim 1 or 2, characterized in that the inflow side of each reaction channel (200, 202) configured as a multiple helix is connected to a dedicated distributor channel (112, 114, 129) and / or mixing section (127).

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

5. Reactor according to any of the preceding apparatus claims, characterized in that the outflow-side collection channel (116) is connected to an outlet throttle and / or outlet nozzle and / or comprises said throttle and / or nozzle.

6. Reactor according to any of the preceding apparatus claims, characterized in that the smallest width of the cross-sectional area (A) of the helix channel (210, 212) is 0.8 mm to 3 mm, ideally 0.8 mm to 2 mm.

7. Reactor according to any of the preceding apparatus claims, characterized in that the cross-sectional area (A) in the helix channel (210, 212) has an elliptical, oval or at least approximately rectangular basic structure, wherein advantageously the ratio of the smallest width (B) to the largest length (H) of the cross-sectional area is not less than 0.5, ideally in the range from 0.2 to 0.06.

8. Reactor according to any of the preceding apparatus claims, characterized in that at least one sensor holder (152) for accommodating and / or securing a sensor (150) is provided, wherein the sensor holder (152) comprises a sensor pier (154) which is connected at one end to a helix channel (210, 212) in the interior (110) and passes through the interior (110) and through the reactor wall of the main body (102) and wherein outside the main body (102) an accommodated and / or secured sensor (150) is connectable in a data-conducting manner to a data receiver.

9. Reactor according to any of the preceding apparatus claims, characterized in that every reaction channel (200) or one helix channel (210, 212) of each reaction channel (200) has a sensor pier (154) of a sensor holder (152) leading to it, in particular a plurality of sensor piers (154) are arranged in the direction of the longitudinal axis (104).

10. Reactor according to any of the preceding apparatus claims, characterized in that each individual helix channel (210, 212) has at least one sensor pier (154) leading to it, inparticular a helix channel (210, 212) of every reaction channel (200, 212) has at least two sensor piers (154) leading to it.11 . Reactor according to any of the preceding apparatus claims, characterized in that the interior (110) comprises at least two separate heat exchange spaces or channels (144) and / or groups of heat exchange channels which are fluidically and spatially separated from one another 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 feed conduit (140) and one discharge conduit (142), wherein each heat exchange space or channel (144, 146) is operable with a different heat transfer medium and / or at its own temperature level.

12. Reactor according to Claim 11 , characterized in that the separating element (146) comprises an insulation layer and / or is at least partially manufactured from a thermally insulating material.

13. Reactor according to any of the preceding apparatus claims, characterized in that the main body has a protective housing arranged around it.

14. Reactor according to Claim 13, characterized in that the protective housing comprises an extraction, a filter unit and / or an absorption unit and / or is connectable thereto.

15. Reactor according to any of the preceding apparatus claims, characterized in that downstream of the at least one inflow-side distributor channel (119, 120) in the direction of the longitudinal axis at least one helix channel (210) of a first reaction channel (200) is combined with at least one helix channel (212) of another reaction channel (202), especially each of the helix channels (210) of the first reaction channel (200) are combined with a respective different helix channel (212) of another reaction channel (202).

16. Reactor according to any of the preceding apparatus claims, characterized in that downstream of the at least one inflow-side distributor channel (119, 120) in the direction of the longitudinal axis the helix channels (210, 210) of at least two reaction channels (200, 202) are passed via a collection unit (132) into a common reaction tube (300), in particular a common reaction tube (300) dimensioned such that the residence time of the reaction mixture in the reaction tube (300)- corresponds to at least 50% of the total reaction duration, in particular- corresponds to at least 75% of the total reaction duration.

17. Plant (500) for performing a synthesis process for producing products from at least two reactants, in particular with a strongly exothermic reaction of liquid reactants, comprising at least one reactor (100), characterized in that the at least one reactor (100) is configured according to any of Claims 1 to 16.

18. Plant (500) according to Claim 17, characterized in that it comprises at least two parallel reactors (100) configured according to any of Claims 1 to 16.

19. Plant according to either of Claims 17 or 18, characterized in that the at least two reactors (100) are connected at the outflow side to at least one common reaction tube (300), in particular to a common reaction tube (300) which is dimensioned such that the residence time of the reaction mixture- corresponds to at least 50% of the total reaction duration, in particular- corresponds to at least 75% of the total reaction duration.

20. Plant according to any 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 comprises the following:- the product conduit (130) as a feed conduit,- a first discharge conduit (402) for the product and / or a substance mixture containing the product and- a gas discharge conduit (404) for volatile substances, wherein the degassing unit is configured such that the pressure (p2) at least in a section within the degassing unit is not more than 2 bar, preferably not more than 1 bar, especially a vacuum of up to 0.5 bar.21 . Production process for a reactor (100) for the synthesis of a product, characterized in that the reactor (100) is configured according to any of Claims 1 to 16 and wherein the reactor (100) is manufactured by means of- a computer-implemented process and- an additive manufacturing process (AMP) via an additive manufacturing apparatus (AMA).

22. Production process according to Claim 21 , characterized in that the AMP is a laser- induced, powder bed-based melting process.

23. Production process according to Claim 21 or 22, characterized in that the computer- implemented process comprises the following steps: a) provision of process data and design parameters for CAD software, b) determination of design data via the CAD software, preferably with at least one determination of strength, in particular via a calculation and / or simulation step according to FEM, c) provision of control data for an additive manufacturing apparatus, d) production of the reactor (100) by the AMA.

24. Storage medium comprising at least one executable program code for performing the production process according to any of Claims 21 to 23 and / or controlling an AMA for performing the production process according to any of Claims 21 to 23.

25. Storage medium according to Claim 24, characterized in that said medium is a storage medium which is integrated in the AMA or connected or connectable to the AMA in a data-conducting manner.

26. Synthesis process for producing a product by a chemical reaction comprising the following steps: a) provision of at least one reactor; b) provision of a first liquid reactant; c) provision of a second liquid reactant, wherein the second reactant may be a substrate which comprises or contains a catalyst; d) provision of a liquid heat transfer medium; e) continuous supplying of the reactor with first reactant, second reactant and heat transfer medium; f) continuous mixing of the first liquid reactant with the second liquid reactant in a mixing section (127) of the reactor (100) to obtain a liquid reaction mixture; g) continuous conversion by reaction of the reactants 1 with the reactant 2, in particular also with the reaction products, downstream of the mixing section (127) and inside the reactor (100) to afford a liquid product mixture and wherein at least a portion of the reaction heat formed during the reaction is transferred from the reaction mixture and / or the product mixture to the heat transfer medium by means of the reactor (100); h) continuous withdrawal of the product mixture from the reactor; i) continuous withdrawal of the heat transfer medium from the reactor, characterized in that the reactor (100) is configured according to any of Claims 1 to 16 and / or the process is performed with / in a plant according to any of Claims 17 to 20.

27. Synthesis process according to Claim 26, characterized in that step e) is preceded by provision of a third reactant (reactant 3) which comprises at least one catalyst or represents a catalyst and wherein the reactants are mixed consecutively, simultaneously or largely simultaneously in step f).

28. Synthesis process according to either of process Claims 26 to 27, characterized in that the (process) pressure (p1) of the reactants is in the range from 10 bar to 100 bar, advantageously in the range from 20 bar to 80 bar, ideally in the range from 35 bar to 65 bar.

29. Synthesis process according to any of process Claims 26 to 28, characterized in that said process comprises a strongly exothermic reaction, in particular a reaction where not less than 70 kJ are released per mole of reactant 1 , preferably not less than 80 kJ are released per mole of reactant 1 , in particular between 85 kJ and 150 kJ are released per mole of reactant.

30. Synthesis process according to any of process Claims 26 to 29, characterized in that the reaction in the reactor (100) forms no volatile byproducts, in particular no volatile byproducts that require continuous removal, in particular that require continuous distillative removal.31 . Synthesis process according to any of process Claims 26 to 30, characterized in that the reaction is selected from the group of the following reactions: a. (poly)addition, b. polymerization of monomers with carbon double bonds (C=C double bonds), c. oxidation of organic compounds, d. esterification, e. Beckmann rearrangement for synthesis of carboxamides.

32. Synthesis process according to process Claim 31 , characterized in that a. the (poly)additions are selected from the group of the following reactions: alkoxylation, ethylene cyanohydrin from HCN and ethylene oxide, urethanes from isocyanates with alcohols or amines, addition reaction of carboxylic acids or carboxylates onto epoxides, hydrogenation reactions, hydrosilylation or hydroformylation; b. the polymerizations of monomers with carbon double bonds (C=C double bonds), in particular free-radical polymerization, are selected from the group of thefollowing reactions: of acrylates, methacrylates, styrene and vinyl compounds, polymerization of butadiene and production of polybutadiene; c. the oxidations are selected from the group of the following reactions:- epoxidation of olefins- oxidation of isobutane to tertiary-buty I hydroperoxide, methanol to formaldehyde, propene to acrolein, acrolein to acrylic acid, ethene to acetaldehyde, acetaldehyde to acetic acid, ethene to acetic acid, cyclohexane to adipic acid,- halogenations,- sulfochlorinations,- nitrations,- Baeyer-Villiger oxidation and- Andrussov process.

33. Synthesis process according to either of process Claims 31 or 32, characterized in that the reaction is an alkoxylation reaction for producing alkoxylates, wherein a) the first liquid reactant is an alkylene oxide selected from the group of: ethylene oxide, (EO), propylene oxide (PO), 1 -butylene oxide (BO), styrene oxide (SO); b) the second liquid reactant is a substrate / a compound selected from the group of: alcohols, fatty alcohols, phenol, alkyl phenols, amines, carboxylic acids and esters thereof, mercaptans and imidazolines and wherein especially the catalyst is a multimetal cyanide complex catalyst or alkali metal or alkaline earth metal hydroxide, in particular sodium hydroxide, potassium hydroxide and caesium hydroxide, or a basic catalyst, for example alkali metal alkoxides, in particular sodium methoxide and potassium methoxide, or a tertiary amine.

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