Rotary raw material processing apparatus with axially adjustable rotor

Abstract

A bladed apparatus (100) for treating feedstock in a process fluid is provided, the apparatus including means for adjusting the position of the working blades of a rotor (3) relative to stator components (2, 4) in the longitudinal direction of a rotor shaft (1). Adjustment is performed by axial displacement of the rotor (3) or alternatively by axial displacement of the reactor shells (22A, 32A). A method for improving treatment efficiency and adjusting flow losses during the treatment of feedstock in a process fluid, particularly under off-design conditions in the bladed apparatus (100), is also provided. In embodiments, the treatment of the feedstock includes thermal cracking or thermochemical cracking of hydrocarbon-containing feedstocks.

Description

Technical Field

[0001] This invention generally relates to the field of rotating turbines with axially adjustable rotors. In particular, the invention relates to an apparatus, related arrangement, method, and use with rotating blades for processing feedstocks such as hydrocarbons. Background Technology

[0002] In the field of turbines, a range of solutions exist that allow rotor units to be displaced in the axial direction. These solutions are typically applicable to axial turbines, such as axial guide vane compressors and turbines, where radial flow losses can be effectively adjusted by axial displacement of the rotor. Radial flow losses are common in annular turbine blade cascades that utilize working fluid to rotate the rotor because the gap between the rotating and stationary components often results in a leakage path (top leakage).

[0003] As an example, DE 101 45 785Al (Ehrenberger) discloses a wind turbine in which, when the rotor's nominal speed is exceeded, the rotor axially moves from its operating position to a lower speed position (in the direction of increasing clearance between the rotor blades and the casing). Axial adjustment solves the problem of stabilizing the rotor speed (rotational speed) under conditions of variable velocity of the inflow fluid.

[0004] None of the above solutions provide any indication of the suitability of the disclosed turbomachinery in the field of chemical processing. An example of an axial reactor is disclosed in U.S. Patent Publication No. 4,288,405 (Koch), constructed for the hydrogenation of dry coal to produce hydrocarbons. This axial reactor has a rotor configured for axial displacement. When the pressure in the hydrogenation chamber exceeds a certain value, the rotor is axially displaced. The movement of the rotor causes the feed inlet into the hydrogenation chamber to close, thereby preventing excessive pressure from diffusing into upstream facilities.

[0005] U.S. Patent Publications 9,494,038 (Bushuev) and 9,234,140 ( (e.g.) discloses a rotary dynamic reactor (RDR) apparatus for converting hydrocarbon feedstocks into light olefins via thermochemical cracking. Generally, the reactor comprises a rotor disk with associated blade cascades disposed between rows of stationary guide vanes arranged on a substantially annular support and enclosed within an annular housing. The process fluid enters the reaction via an inlet and passes through the stator and rotor blade cascades several times along a substantially helical trajectory before exiting the reactor.

[0006] Low-molecular-weight olefins (such as ethylene, propylene, and butene) are major components of the petrochemical industry and are used as essential building blocks in the commercial production of plastics, polymers, elastomers, rubber, foams, solvents, chemical intermediates, and fibers (including carbon fibers) and coatings. Compared to conventional tubular pyrolysis furnaces, the aforementioned rotary-powered machines allow for thermochemical reactions with shorter residence times and improved controllability of the cracking process, which is generally associated with increased yields of the target product and prevention of said product from secondary reactions.

[0007] A common problem with known RDR solutions is flow leakage along the circumferential direction (also known as the tangential or ring direction). In practice, leakage occurs in the direction from the inlet to the outlet (instead of entering the reaction zone) and / or in the direction from the end of the reaction zone to the beginning of the adjacent reaction zone (instead of leaving the reactor), caused by operating the reactor under conditions different from the nominal conditions (in a so-called non-design mode).

[0008] For completeness, we note that the leakage problem in the aforementioned directions (inlet to outlet; end of the reaction zone to the start of the adjacent reaction zone) is not encountered in conventional axial flow solutions.

[0009] Therefore, leakage is unavoidable when operating the reactor under variable flow rate and / or feed-related conditions. Similarly, leakage occurs when the temperature inside the reactor is changed (while all other parameters remain constant), as this is related to adjusting the rotor's rotational speed.

[0010] This leakage flow leads to a reduction in total mass flow and work transfer, and negatively impacts reactor stability, narrowing its operating range—that is, its ability to operate within a limited range of fluid flow rates and rotational speeds. Furthermore, flow leakage results in coke formation and significantly reduces the yield of the target product. Therefore, these adverse effects impact the reactor's industrial applicability, its attractiveness to end users, and its market potential.

[0011] In practice, the only way to prevent leakage is to operate the RDR equipment with a unique combination of the mass flow rate through the reactor and the rotational speed of the rotor, wherein a predetermined rotational speed is assigned to a certain mass flow rate while the feed composition remains constant.

[0012] The solution proposed by Bushuev in US 9,494,038 B2 suggests adjusting the geometry of the stationary guide vane cascade in the circumferential direction to achieve pressure equalization at the inlet and outlet of the rotor guide vane cascade throughout the entire cascade, where the reactor operates under nominal design conditions. Additionally, the position of the stator guide vane cascade can be adjusted, but only in the circumferential direction relative to the rotor axis of rotation. The proposed arrangement aims to mitigate undesirable large-scale mixing between adjacent flows. However, this disclosure does not address the problem of reducing leakage under off-design operating conditions.

[0013] In this regard, given the challenges associated with preventing or at least minimizing flow leakage, updates are still needed in the field of improving the efficiency of rotary reactor equipment (especially RDR type rotary reactor equipment) for chemical processing of hydrocarbon feedstocks in order to optimize the operating range and efficiency of reactors under variable processing conditions. Summary of the Invention

[0014] The object of this invention is to solve or at least mitigate each problem caused by the limitations and disadvantages of related technologies. This object is achieved through various embodiments of apparatus, related arrangements, methods, and uses for treating raw materials in a process fluid. Therefore, in one aspect of the invention, an apparatus for treating raw materials in a process fluid as defined in independent claim 1 is provided.

[0015] In one embodiment, the device includes: a rotor comprising a plurality of rotor blades arranged circumferentially on a disk mounted to a rotor shaft and forming a rotor blade cascade; a plurality of stationary guide vanes arranged in a substantially annular cascade of guide vanes, the guide vane cascade being disposed adjacent to the rotor blade cascade to form a stator-rotor-stator arrangement; and a housing having a conduit formed therein, the conduit having at least one inlet and at least one outlet, the housing enclosing the rotor blade cascade and the stationary guide vane cascade inside the conduit, wherein the position of the rotor blade cascade relative to the stationary guide vane cascade in the stator-rotor-stator arrangement is adjustable along the rotor shaft in the axial direction by a predetermined distance (ΔX).

[0016] In an embodiment, the position of the rotor blade cascade relative to the stationary guide vane cascade in the stator-rotor-stator arrangement can be adjusted by axially shifting the rotor in the longitudinal direction of the rotor shaft.

[0017] In one embodiment, the device further includes at least one thrust bearing element disposed on the rotor shaft, wherein the rotor is axially displaced by axial displacement of the at least one thrust bearing element on the rotor shaft.

[0018] In an embodiment, the at least one thrust bearing element is configured to be axially displaced relative to the (reactor) housing.

[0019] In one embodiment, the thrust bearing element is housed in a separate housing that is at least partially enclosed within the bearing housing, and wherein the enclosed thrust bearing element is configured to be axially displaced in the longitudinal direction of the rotor shaft within the associated bearing housing.

[0020] In this embodiment, the coupling disposed between the rotor shaft and the drive shaft is a flexible shaft coupling, which is configured to allow axial displacement of the drive shaft and / or the rotor shaft. Therefore, the flexible coupling allows axial displacement of the drive shaft and / or the rotor shaft.

[0021] In some embodiments, the rotor is axially displaced by axial displacement of a drive shaft connected to the rotor shaft via a coupling.

[0022] In some embodiments of the device, the position of the rotor blade cascades relative to the stationary guide vane cascades in the stator-rotor-stator arrangement can be adjusted by axially displacing at least one stationary component, particularly the (reactor) housing, in the longitudinal direction of the rotor shaft. The drive shaft is preferably fixed, thereby preventing axial displacement of the drive shaft.

[0023] In some other embodiments, the coupling disposed between the rotor shaft and the drive shaft is a rigid coupling, which is configured to prevent the drive shaft and the rotor shaft from shifting axially.

[0024] In one embodiment, each of the plurality of stationary guide vane cascades is fixed to a corresponding bearing housing arranged on both sides of the reactor (gas) casing.

[0025] In an embodiment, the device is configured such that adjusting the position of the rotor blade cascade in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is accompanied by at least adjusting the rotational speed of the rotor and / or the flow rate of the processing fluid containing the raw material.

[0026] In one embodiment, the device further includes a flow forming apparatus disposed inside the (gas) housing, such that a conduit is formed between the outer housing and the flow forming apparatus, the conduit having an annular meridional cross-section. In another embodiment, the flow forming apparatus is an annular, substantially hollow structure.

[0027] In one embodiment, in the device, a vaneless space is formed between the outlet of the stator-rotor-stator arrangement and the inlet of the stator-rotor-stator arrangement, the vaneless space being defined by a volume portion between the (gas) casing and the flow forming device.

[0028] In one embodiment, the stationary guide vane cascade is formed with a plurality of stationary nozzle guide vanes and a plurality of stationary diffuser guide vanes. The plurality of stationary nozzle guide vanes form an annular nozzle guide vane cascade upstream of the rotor blades, and the plurality of stationary diffuser guide vanes form a diffuser guide vane cascade downstream of the rotor blades.

[0029] In an embodiment, the vanes in the stator-rotor-stator arrangement are configured to guide the process fluid through the vanes and through the vaneless space according to a helical flow path as it is conveyed in the pipe between at least one inlet and at least one outlet, and are configured to establish conditions for at least one chemical reaction to occur in the process fluid.

[0030] In one embodiment, the device also includes multiple catalytic surfaces.

[0031] In some other aspects, according to the contents defined in independent claims 19 and 20, use of the apparatus for processing feedstocks in a processing fluid is provided according to embodiments. In embodiments, the use is provided in the thermal treatment of (multiple) hydrocarbon-containing feedstocks. Additionally or alternatively, the use is provided for carrying out chemical reactions. In embodiments, the use is provided for the thermal cracking or thermochemical cracking of (multiple) hydrocarbon-containing feedstocks.

[0032] In an embodiment, the use is provided for performing at least one process selected from the group consisting of: processing a hydrocarbon feedstock preferably containing medium-weight and light hydrocarbon fractions; processing a gasified carbohydrate-containing feedstock; processing a gasified feedstock containing glycerides and / or fatty acids; and processing a gasified cellulosic biomass material.

[0033] On the other hand, according to the definition in independent claim 23, an arrangement of the apparatus for treating a raw material in a processing fluid is provided according to an embodiment. In this arrangement, at least two devices are functionally connected in parallel or in series.

[0034] In another aspect, according to the content defined in independent claim 24, a method is provided for improving processing efficiency and adjusting flow losses during the processing of a feedstock in a processing fluid. In an embodiment, the method includes:

[0035] - Obtaining an apparatus comprising: a rotor including a plurality of rotor blades arranged circumferentially on a disk mounted to a rotor shaft and forming a rotor blade cascade; a plurality of stationary guide vanes arranged in an annular guide vane cascade, the annular guide vane cascade being arranged adjacent to the rotor blade cascade to form a stator-rotor-stator arrangement; and a housing having a conduit formed therein, the conduit having at least one inlet and at least one outlet, the housing enclosing the rotor blade cascade and the stationary guide vane cascade inside the conduit; and

[0036] - Adjust the position of the rotor blade cascade in the stator-rotor-stator arrangement relative to the stationary guide vane cascade by a predetermined distance (ΔX) in the axial direction along the rotor shaft.

[0037] In one embodiment, the position of the rotor blade cascade relative to the stationary guide vane cascade in the stator-rotor-stator arrangement is adjusted by axially shifting the rotor in the longitudinal direction of the rotor shaft.

[0038] In another embodiment, the position of the rotor blade cascade relative to the stationary guide vane cascade in the stator-rotor-stator arrangement is adjusted by axially displacing at least one stationary component, particularly the housing, in the longitudinal direction of the rotor shaft.

[0039] According to each specific embodiment of the invention, the utility of the invention stems from various reasons. By providing a rotor that is displaceable in the axial direction (i.e., in the longitudinal direction of the rotor shaft), flow losses associated with tip gap leakage, characteristic of known rotary reactors and / or turbines, can be effectively prevented or at least minimized. In conventional rotary reactors, flow leakage triggers a series of secondary reactions, leading to the formation of byproducts (such as coke) and reducing the yield of the primary (target) product.

[0040] This invention has proven particularly advantageous for attempting to operate rotary reactor equipment designed for (thermo)chemical reactions (such as (steam) cracking of hydrocarbons) in a non-designed mode, established when varying ranges of parameters within the reactor (e.g., processing temperature and / or feedstock chemical composition, typically associated with adjusting the rotor's rotational speed). The resulting solution may be essential, for example, for use in cracking facilities or any other related facilities operating with different feedstocks.

[0041] By utilizing a movable rotor solution, the operation of a conventional rotary reactor unit can be optimized, at least in terms of efficiency, for multiple operating conditions different from those assigned to the design model. Accordingly, the operational range of the reactor and related facilities (e.g., cracker units) can be extended.

[0042] Rotor shifting solutions are flexible and can be effectively used in the design of equipment for (thermal) chemical feedstock processing (RDR solutions, axial flow solutions, etc.) as well as in rotating turbines.

[0043] The terms “pyrolysis” and “cracking” are used in this disclosure primarily as synonyms for the treatment of thermally degrading a heavier hydrocarbon compound into a lighter hydrocarbon compound.

[0044] The expression “several” here refers to any positive integer starting from one (1), such as one, two, or three. The expression “multiple” here refers to any positive integer starting from two (2), such as two, three, or four.

[0045] Unless otherwise expressly stated, the terms “first” and “second” are used herein only to distinguish one element from another and do not indicate any particular order or importance.

[0046] In this disclosure, the terms "fluid" and "processing fluid" primarily refer to gaseous substances, such as gaseous feedstock streams that are preferably guided through the interior of a reactor device in the presence of a diluent.

[0047] The term “gasified” is used in this article to refer to substances that are converted into a gaseous form by any possible means.

[0048] The term "fluid dynamics" is used herein to refer to the power of a fluid, which in this disclosure is primarily represented by a gas. Therefore, the term is used in this disclosure as a synonym for the term "gas dynamics."

[0049] Various embodiments of the invention will become apparent from consideration of the detailed description and accompanying drawings. Attached Figure Description

[0050] Figure 1 The stator-rotor-stator arrangement in device 100 operating under design conditions is shown.

[0051] Figures 2 to 5 The velocity triangle and stator-rotor-stator arrangement in a device 100, which operates at least partially under non-design conditions and displaces the rotor relative to the stator elements by a predetermined distance ΔX according to an embodiment, are shown.

[0052] Figure 6A This is a vertical cross-sectional view of the device 100 according to an embodiment. Figure 6B Showing cross Figure 6A The cross-sectional views of lines AA and BB specified above are shown, and a flow diagram through the streamlined channel of device 100 is also shown.

[0053] Figure 7 The velocity triangle and stator-rotor-stator arrangement in a device 100, which operates under both design and non-design conditions and causes the rotor to shift a predetermined distance ΔX relative to the stator elements, are illustrated according to an embodiment.

[0054] Figures 8A to 8C Different arrangements for axial rotor displacement according to embodiments are shown.

[0055] Figure 9 This is a vertical cross-sectional view of device 100, showing an exemplary mechanism for axial rotor displacement. Detailed Implementation

[0056] Detailed embodiments of the invention are disclosed herein with reference to the accompanying drawings. The same reference numerals are used throughout the drawings to refer to the same components.

[0057] Figure 6A The concept on which various embodiments of a reactor apparatus (hereinafter referred to as reactor) for processing raw materials in a process fluid (working fluid) are based is shown in 100. Figures 8A to 8C and Figure 9 Reactors 100 (100A, 100B, 100C) according to embodiments are shown.

[0058] The implementation of device 100 generally follows U.S. Patent Publications 9,494,038 (Bushuev) and 9,234,140 (…). The guidelines established in (etc.), these two U.S. patents are incorporated herein by reference and describe a rotating turbine type reactor in which both the rotor structure and the stator structure are enclosed in a substantially annular shell.

[0059] The reactor 100 is preferably configured to process feedstock, such as hydrocarbon-containing feedstock, by carrying out at least one chemical reaction in the processing fluid, and then convert the feedstock into the desired product.

[0060] In the selected configuration, the reactor is constructed for the thermal or thermochemical conversion of hydrocarbon feedstocks, particularly fluidized hydrocarbon feedstocks. "Hydrocarbon feedstock" here refers to fluidized organic feedstock substances that primarily consist of carbon and hydrogen. However, in some cases, the reactor may be constructed to process oxygen-containing feedstock substances, such as oxygenated hydrocarbon derivatives, cellulose-based feedstocks, and / or vegetable oil-based feedstocks. Therefore, the applicability of the proposed reactor goes beyond the limitations imposed by the conventional definition of hydrocarbon feedstocks.

[0061] The hydrocarbon-containing feedstock entering the reactor is provided in a substantially fluid form (such as liquid or gas). In a preferred configuration, reactor 100 is designed to process gasified feedstocks, wherein the processing fluid is provided in gaseous form. In alternative configurations, processing substantially liquid feedstocks is not excluded.

[0062] Therefore, reactor equipment 100 is suitable for use in the heat treatment of hydrocarbon-containing feedstocks. The heat treatment preferably involves the conversion of the feedstock into (multiple) desired products, thereby establishing conditions for at least one chemical reaction to occur in the treatment fluid. Alternatively, the treatment conditions in equipment 100 can be adjusted such that conditions for chemical change (reaction) are not established during the heat treatment, thereby giving the equipment (pre)heater functionality.

[0063] In the embodiments, apparatus 100 is adapted for thermal and / or thermochemical hydrocarbon degradation reactions, such as pyrolysis, which together cause the cracking of hydrocarbon-containing feedstock and are optionally assisted by a dilution medium (diluent). Therefore, reactor 100 can be adapted for pyrolysis reactions with or without a dilution medium. Furthermore, the presence of a dilution medium is preferred because it increases product yield.

[0064] Reactor 100 can be configured to receive feedstock diluted with at least one diluent (preferably a gaseous diluent, such as steam). In steam cracking processes, steam is preferred as the diluent because it lowers the partial pressure of hydrocarbons, thus inhibiting or reducing the formation of coke deposits through the gasification reaction(s). In some cases, the diluent is an inert gaseous medium, such as hydrogen (H2), nitrogen (N2), or argon, which has essentially zero reactivity to the reactants and products. The use of any other suitable diluent is not excluded. In some cases, dilution is used to lower the partial pressure and improve the efficiency of the cracking reaction, which is beneficial for the production of desired olefins (e.g., ethylene and propylene). In some other cases, reactor 100 can operate without a diluent.

[0065] In some configurations, device 100 is a steam cracking reactor.

[0066] Reactor 100 includes a rotor system (hereinafter referred to as rotor) comprising a shaft 1 positioned along a horizontal (longitudinal) axis X-X' and rotor units mounted on the shaft 1. Reactor 100 also includes at least one drive engine unit 1C (see [link to relevant documentation]). Figures 8A to 8C The reactor 100 can utilize various drive engines, such as electric motors, or the reactor can be directly driven by a gas turbine or steam turbine. A suitable coupling 1A is arranged between the drive shaft 1B and the rotor shaft 1 (see [link]). Figures 8A to 8C Depending on the configuration, both flexible and rigid (non-flexible) couplings 1A can be used. The rotor shaft 1 is supported by relevant bearing components, which will be discussed further below.

[0067] The rotor unit includes multiple rotor blades 3 (also called working blades) arranged circumferentially on a disk 3a mounted to a rotor shaft 1. The multiple rotor blades arranged on the disk together form a rotor blade assembly or rotor blade cascade (rotor blade cascade 3). The rotor blades 3 may be configured with an axial flow blade profile, where the term "axial flow" generally indicates that the processing fluid enters the rotor blade cascade from a direction substantially perpendicular to the rotor rotation direction. Each rotor blade has a side surface with concave curvature (concave side) and a side surface with convex curvature (convex side). In the rotor blade cascade, the working blades are mounted on the rotor disk, with the concave side of each blade arranged along the rotor rotation direction, such as... Figure 1 The arrow shape is shown in the image. In each working blade (top view outline, as shown in the image),... Figure 1 In what we see, the direction from the convex side to the concave side is the rotor rotation direction. As an example, rotor blades can be constructed with a supersonic turbine blade profile.

[0068] The term "blade cascade" (the crown of blades / guide vanes) refers to the entirety of (working) blades or (stationary) guide vanes mounted on the periphery of the rotor disk or on an annular support or housing.

[0069] The reactor 100 also includes a stationary component. The stationary component is represented by a plurality of stationary (stator) guide vanes 2, 4, which are arranged in a substantially annular assembly or cascade (stator vane cascade 2, 4) on both sides of the bladed rotor disk. Thus, the first stator vane cascade 2 is located upstream of the rotor vane cascade 3, and the second stator vane cascade 4 is located downstream of the rotor vane cascade.

[0070] The terms “upstream” and “downstream” here refer to structural portions or components relative to predetermined portions or components (in this case, rotor disks with associated blades), substantially in the direction of fluid flow throughout the reactor (e.g., along axis X-X’, as shown). Figure 6A , Figures 8A to 8C and Figure 9 (as shown) spatial and / or functional layout.

[0071] The stationary guide vanes are arranged adjacent to the rotor blades to form a stator-rotor-stator arrangement (SRSA) 2, 3, 4. When the reactor operates under design conditions, the distances between the rotor and stator components in the SRSA can be substantially the same.

[0072] The vane cascade arranged upstream of the rotor disk includes multiple nozzle guide vanes (NGVs), also known as nozzle guide vanes. These guide vanes form an annular nozzle guide vane cascade 2. The vane cascade arranged downstream of the rotor disk includes multiple diffuser guide vanes, also known as outlet guide vanes, which form an annular diffuser vane cascade (diffuser).

[0073] The first stationary guide vane 2 and the second stationary guide vane 4 have curved profiles, which are preferably adjusted for supersonic flow velocities passing through the associated blade cascade. In the reactor 100, the stationary guide vanes are mounted such that the convex side of each vane is arranged along the rotor rotation direction. Therefore, in each stationary guide vane (top view profile, such as...), Figure 1 In what we see, the direction from the concave side to the convex side is the direction of rotor rotation.

[0074] The reactor 100 also includes a housing 6, in which an internal passage is formed in the form of a pipe having at least one inlet 8 and at least one outlet 9. For the purposes of this invention, the housing 6 is considered a stationary component. In this context, the term "stationary" is used in the meaning of "non-rotational"; the possibility of (axial) displacement is not excluded, as further explained below.

[0075] Figure 6A A reactor configuration with two inlets 8A, 8B and two outlets 9A, 9B is shown; other configurations are conceivable where appropriate. As an example, the reactor may include one inlet and one outlet; one inlet together with two outlets or two inlets together with one outlet. Reactors with a greater number of inlets and / or outlets can be implemented. The inlets and outlets include associated openings / ports in the housing 6 and pipes, sleeves, or manifolds associated with each said port.

[0076] The outer casing 6 is configured to substantially completely surround the periphery of the rotor disk, on which the working blades are assembled, and the stationary guide vane cascades 2, 4 are adjacent to the rotor blades and together form the stator-rotor-stator arrangements 2, 3, 4. The outer casing 6 has a substantially annular shape (“ring” shape) in a three-dimensional configuration, whereby the rotor system (1, 3A, 3) with associated bearing assemblies can be considered as a hole filling the opening in the central portion defining the annular shape. The annular structure is also referred to as a gas casing. The gas casing 6 is substantially annular in its meridional section.

[0077] The reactor also includes a flow shaping device (guide device) 5 disposed inside the gas casing 6. The flow shaping device 5 can be configured as an internally stationary annular structure, and serves to create a substantially annular channel inside the casing 6. The device 5 is secured to the gas casing 6 by suitable fasteners (not shown). In some configurations, for example, the flow shaping device 5 is an annular, substantially hollow structure, such as a ring clamp.

[0078] The internal volume of the reactor is defined as the space established between the gas shell 6 (outer “annular chamber”) and the internal flow shaping device 5 (inner “annular chamber”).

[0079] Therefore, a substantially annular channel / pipe is formed between the inner surface of the gas casing 6 and the outer surface of the flow forming device 5. Accordingly, this pipe has an annular meridional cross-section. The flow forming device 5, configured as an internal ring, is located adjacent to the tips of the rotor blades (forming a gap between them, allowing the rotor to rotate unimpeded) and the peripheral portion of the stator guide vanes. In some configurations, the stationary guide vane cascades 2, 4 may be mounted on the bearing housings of the bearing system, which constitutes the rotor and will be discussed further below.

[0080] In some other cases, the stator vane cascade can be assembled on the flow forming apparatus 5 adjacent to the rotor blades 3. Therefore, the stator guide vanes can be mounted on the flow forming apparatus and / or connected to it via auxiliary devices (such as rings, supports, etc. (not shown)). The above features are described in Bushuev (US 9,494,038 B2) and... The above is discussed in more detail in the public documents (US 9,234,140), which represent the closest prior art and are cited above.

[0081] Within the gas casing 6, vanes 2, 3, and 4 are adjacent to each other, creating a vaneless space 7 between the outlet of the stator-rotor-stator arrangement (i.e., the outlet of diffuser vane 4) and the inlet of the same arrangement (i.e., the inlet of nozzle guide vane 2). This vaneless space is formed between the inner surface of the gas casing 6 and the outer surface of the flow forming apparatus 5. Most of the chemical reactions that trigger the conversion of (multiple) raw materials into the target product occur within this vaneless space.

[0082] Multiple working chambers are formed inside the reactor by arranging partitions (not shown) within the aforementioned annular channel / pipe. The partitions are arranged symmetrically about the rotor's axis of rotation. This allows for reactor configurations involving, for example, two or four working chambers. Preferably, the inlet ports are arranged after each partition (in the rotor's direction of rotation), while the outlet ports are arranged before each partition. In some cases, the annular channel can be implemented without partitions.

[0083] In the above configuration, the process fluid flow is configured to be delivered in a pipe forming the interior of the reactor according to a helical trajectory. Blades 2, 3, 4 forming a stator-rotor-stator arrangement guide the process fluid repeatedly through the blades and through the vaneless space 7, thereby establishing a helical flow path in a substantially annular pipe between at least one inlet and at least one outlet.

[0084] In operation, the (stationary) nozzle guide vane 2 is configured to direct the process fluid flow into the rotor blades. Provided as a stationary structure, the stator does not add energy to the process fluid. However, in terms of its profile, dimensions, and arrangement around the rotor shaft 1, the nozzle guide vane is configured to direct the process fluid flow into the rotor blades in a predetermined direction in order to control and, in some cases, maximize the rotor's specific work input capability.

[0085] The processed fluid flow further enters multiple rotor blades 3, which are configured to receive the fluid flow from the stationary guide vanes 2 as the rotor rotates and add mechanical energy to the processed fluid by increasing the velocity of the fluid flow. Accordingly, the increased flow velocity increases the kinetic energy of the fluid. The velocity of the flow through the stator-rotor-stator arrangement is essentially supersonic.

[0086] The stationary diffuser 4 with guide vanes reduces the flow velocity and kinetic energy of the processed fluid, thereby allowing the fluid to enter the vaneless space 7 at subsonic speeds.

[0087] During the residence time inside reactor 100, the process fluid passes through blades 2, 3, and 4 several times, and each time it passes through rotor blade cascade 2, the process flow is accelerated, thus receiving the kinetic energy dissipated into the internal energy of the (multiple) reaction (processing) fluid as it passes through diffuser 4 and the vaneless space 7, thereby providing the thermal energy required to break down the chemical bonds between long carbon-hydrogen (CH) chains. The increase in the internal energy of the fluid leads to an increase in fluid temperature. Therefore, the size of high molecular weight compounds present in the process fluid is effectively reduced.

[0088] Therefore, as the processing fluid flows through the stationary nozzle guide vane cascade 2, rotor blade cascade 3, stationary diffuser guide vane cascade 4, and reaches the guide vane-free space 7, a processing stage configured as an intermediate complete energy conversion cycle is established. During the energy conversion cycle, the fluid's mechanical energy is converted into kinetic energy and further into the fluid's internal energy, subsequently increasing the fluid temperature and causing chemical reactions within the fluid.

[0089] During the residence time within reactor 100, the process fluid follows a helical path through the vane cascade and the vaneless space, thus establishing multiple processing stages (typically 5-10) during one processing cycle. The processing cycle is defined by a time period during which the flowing particles, along with the process stream, are transferred from reactor inlet 8 to outlet 9, accompanied by the conversion of the feed compound into the target product. Pyrolysis processes, including (steam) cracking, require high temperatures and are highly endothermic; therefore, the reaction is carried out at high temperatures (750°C-1000°C, typically 820°C-950°C), where the residence time in the reaction zone is on the order of fractions of a second, such as about 0.5-0.1 seconds and as low as 0.03-0.01 seconds (30-10 milliseconds). For completeness, we note that the feed-containing process fluid entering the reactor is preheated to about 500-600°C.

[0090] Residence time affects the ratio of primary to secondary products at constant temperatures. Therefore, short residence times allow primary reactions that form the target product (such as light olefins available in steam cracking) to dominate; while longer residence times increase secondary reactions, leading to coke formation.

[0091] Overall, reactor 100 is configured, in terms of its geometry and stator and rotor parameters, to establish conditions for at least one chemical reaction to occur in the processed fluid.

[0092] As the feedstock (multiple components) is conveyed through the reactor along a spiral path as described above, the processing fluid entering the reactor undergoes a transformation to form the target product, which exits the reactor as a fluid effluent. During the processing cycle, processing conditions may need to be adjusted to promote the primary reactions that form the target product, while avoiding or at least minimizing secondary reactions that typically result in coke formation.

[0093] The present invention is based on the observation that when the position of the rotor blade cascade 3 in the stator-rotor-stator arrangement relative to the stationary guide vane cascade 2 and 4 is adjusted in the axial direction of the rotor shaft (i.e., in the longitudinal direction along the axis X-X' of the rotor shaft 1), the flow loss generated in the circumferential direction during rotor rotation, especially flow leakage, can be adjusted with high efficiency.

[0094] Therefore, the present invention is based on adjusting the distance between the rotor blade cascade 3 and the stationary guide vane cascades 2 and 4 along the longitudinal direction of the axis (X-X') defined by the rotor shaft. In some configurations, the position of the rotor blade cascade relative to the stationary guide vane cascade can be adjusted by allowing the rotor to be displaced in the axial direction (see [link]). Figure 8A , Figure 8B , Figure 9 ).

[0095] In some alternative configurations, the position of the rotor blade cascade relative to the stationary guide vane cascade can be adjusted by axial displacement of one or more stationary components. In some embodiments, the displaceable stationary component is the reactor shell 6 (see...). Figure 8C ).

[0096] In Bushuev and In rotary machine-type reactors as described in relevant patent disclosures, in most cases, changes in any of the following—the feed composition, feed consumption rate, equipment-related parameters, and / or processing-related parameters (e.g., rotor speed, temperature, pressure, etc.)—cause fluctuations in the fluid flow conveyed through the reactor and the formation of circumferential leaks. Specifically, leaks form in the direction from the inlet to the outlet or from the end of the reaction zone to the beginning of the adjacent reaction zone. For example, increasing the processing temperature (where the chemical composition and mass flow rate of the processing fluid containing the feed are substantially constant) is generally associated with the need to increase the rotor speed. However, this results in flow leakage from the end of the reaction zone back to the beginning of the adjacent reaction zone (see also...). Figure 3 (B), which in turn may lead to coke formation and significantly reduce the yield of the target product.

[0097] Return to reference Figure 1 This diagram illustrates the arrangement of stator guide vanes 2, 4 relative to rotor blades 3 in reactor 100 operating under design conditions. The design operating mode involves rotating the rotor at a design rotational speed U (also known as peripheral (circumferential) or tangential speed). The direction of rotation of the rotor about its axis is indicated by arrow shapes. For completeness, speed is defined as velocity in the relevant direction; otherwise, the terms "speed" and "rate" are used interchangeably.

[0098] Figure 1 The velocity triangles (V1, W1, α1, β1) of the fluid flow leaving the nozzle guide vane 2 and entering the rotor vane 3, and the velocity triangles (V2, W2, α2, β2) of the fluid flow leaving the rotor vane 2 and entering the diffuser vane 4 are shown, where V is the absolute velocity of the fluid flow, W is the relative velocity of the fluid flow, α1 (alpha 1) is the angle at which the absolute fluid flow (V1) enters the rotor vane, α2 (alpha 2) is the angle at which the absolute fluid flow (V2) enters the stationary diffuser guide vane, β1 (beta 1) is the angle at which the relative fluid flow (W1) enters the rotor vane, and β2 (beta 2) is the angle at which the relative fluid flow (W2) leaves the rotor vane and enters the stationary diffuser guide vane.

[0099] The inlet of the blade / guide vane cascade is generally defined by the leading edge of the associated blade / guide vane, while the outlet of the cascade is defined by the trailing edge of the blade / guide vane. The inlet and outlet are defined in the direction of fluid flow.

[0100] Figures 2 to 5 The stator-rotor-stator arrangement in reactor 100, operating at least partially under non-design conditions, is schematically shown. Velocities W1 and V2 are indicated by dashed arrows.

[0101] A reactor operating under design conditions (so-called design model) is defined as a reactor whose geometry is designed and optimized to achieve predetermined input-related conditions in practice, wherein the inputs may involve the state of the fluid being processed (pressure, temperature, mass flow rate of the fluid being processed), the system (rotor speed, external temperature regulation, etc.) and / or the feedstock (predetermined loading rate, chemical composition, etc.).

[0102] Non-design conditions refer to conditions where the inputs used in practice differ from those designed for the system's operation. Non-design operation can be characterized by: operating at temperatures, pressures, and / or mass flow rates different from design point parameters; operating the system under varying loads and / or with different feedstocks.

[0103] Figure 2 Figure A shows the velocity triangle under operating conditions involving a rotor rotational speed (U') lower than the rotor rotational speed (U) in the design mode; while Figure 3 A shows the velocity triangle under operating conditions involving a rotor rotational speed (U') that is higher than the rotor rotational speed (U) in the design mode.

[0104] Figure 4 Figure A shows the velocity triangle under operating conditions involving the rotor rotational speed (U) in the design mode, but with increased flow rate (and therefore, increased mass flow rate, involving greater consumption of feed material flowing through the reactor). In this case, the absolute velocity (V1') of the fluid flow leaving the nozzle guide vanes and entering the rotor vanes will be greater than the absolute velocity (V1) in the design mode.

[0105] Accordingly, Figure 5 Figure A shows the velocity triangle under operating conditions involving the rotor rotational speed (U) in the design mode, but with reduced flow rate (and therefore, reduced mass flow rate, resulting in less consumption of feed material flowing through the reactor). In this case, the absolute velocity (V1') of the fluid flow leaving the nozzle guide vanes and entering the rotor vanes will be less than the absolute velocity (V1) in the design mode.

[0106] therefore, Figures 2 to 5 This shows the velocity triangle (V1) achievable for the fluid flow exiting the nozzle guide vanes and entering the rotor vanes in reactor 100 operating under non-design conditions different from the design conditions. ’ W1 ’ α1 ’ β1 ’ ) and the velocity triangle (V2) obtainable for the fluid flow leaving the rotor blades and entering the diffuser blades. ’ W2 ’ α2 ’ β2 ’), where V ’ is the absolute velocity of the fluid flow, and W ’ is the relative velocity of the fluid flow, and α1 ’ (alpha 1 ’ ) is the angle at which the absolute fluid flow (V1 ’ ) enters the rotor blade, and α2 ’ (alpha 2 ’ ) is the angle at which the absolute fluid flow (V2 ’ ) leaves the rotor blade and enters the stationary diffuser vane, and β1 ’ (beta 1 ’ ) is the angle at which the relative fluid flow (W1 ’ ) enters the rotor blade, and β2 ’ (beta 2 ’ ) is the angle at which the relative fluid flow (W2 ’ ) leaves the rotor blade and enters the stationary diffuser vane.

[0107] Table 1 presents fluid flow related parameters for operating the reactor 100 in the design mode (U, V, W, α, β) and the off-design mode (U’, V’, W’, α’, β’).

[0108] Table 1 . Comparison of fluid flow related parameters under design conditions and off-design conditions ( Figures 2 to 5 ).

[0109]

[0110] Based on the velocity triangle ( Figures 2 to 5 A), a processed fluid flow transmission path (streamline) through the rotor blade has been generated in the reactor inlet region (inlet 8) and the reactor outlet region (outlet 9).

[0111] Figures 2 to 5 B, Figure 5 C shows the effect of the axial shift of the rotor on adjusting the flow leakage in the reactor operating under off-design conditions. Similar provisions apply when the distance between the rotor cascade and the stationary cascade in the stator-rotor-stator arrangement is changed by the axial shift of the housing.

[0112] Figure 2 B shows the flow transmission paths at the design rotational speed (U; the relevant streamlines are shown by dashed lines) and the off-design rotational speed (U’), where the off-design rotational speed is lower than the design rotational speed (the relevant streamlines are indicated by U’ < U). From Figure 2 B, it can be observed that at the reduced rotational speed U’, a portion of the fluid flow is directly transmitted from the inlet 8 of the reactor to the outlet 9 of the reactor.

[0113] As seen from Figure 2 B of Figure 2 , reducing the rotor rotation speed results in leakage in the inlet-to-outlet direction, where some of the process stream does not enter the reaction zone. In the pyrolysis reaction, this naturally leads to a reduction in the yield of the main (target) product. When the temperature in the reactor decreases, the rotation speed of the rotor typically decreases. Other process parameters (such as the chemical composition of the process fluid containing the raw material and the mass flow rate of the process fluid through the reactor) remain substantially constant.

[0114] Figure 2 C of

[0114] shows the following situation: wherein the rotor cascade 3 is displaced a predetermined distance ΔX (Delta X) in the direction of the nozzle guide cascade 2 by displacing the rotor, i.e., the displacement distance. By displacing the rotor, the associated cascade 3 is displaced a distance ΔX from its original position occupied by the cascade in the design mode. The displacement of the rotor occurs in the axial direction along the axis X-X' (see Figure 6A , Figures 8A to 8C , Figure 9 ). The displacement amplitude defined by the value ΔX is selected such that when the rotor is moved by said value, substantially all of the flow stream travels from the inlet 8 of the reactor towards the start of the reaction zone (at a rotational speed U' < U).

[0115] Referring to Figures 2 to 5 and Figure 7 , the reaction zone is defined by the region formed in the duct between the gas casing 6 and the flow shaping device 5, wherein the main chemical reaction(s) for forming the target product occur during the process cycle as defined above. For clarity, we note that most of the chemical reactions occur in the region / volume occupied by the vaneless space.

[0116] Figure 3 B of

[0116] shows the flow transfer paths at the design rotational speed (U; the relevant streamlines are shown by dashed lines) and the off-design rotational speed (U'), wherein the off-design rotational speed is higher than the design rotational speed (see streamlines U' > U). From Figure 3 B of Figure 3 , it can be observed that at the increased rotational speed U', a portion of the flow stream is transferred back from the end of the reaction zone to the start of the reaction zone.

[0117] As seen from Figure 3As seen in section B and the above overview of the rotary power equipment constituting the prior art, increasing the rotor speed results in leakage in the direction from the end of the reaction zone back to the beginning of the adjacent reaction zone, where the newly formed primary product returns to the beginning of the reaction zone instead of leaving the reactor. This leads to the formation of secondary reaction products, such as coke, thereby correspondingly reducing the yield of the target product. The rotor speed is typically set to a larger value as the temperature in the reactor increases. As in the previous example, other processing parameters (such as the chemical composition of the processing fluid containing the feedstock and the mass flow rate of said processing fluid through the reactor) remain substantially constant.

[0118] Figure 3 C illustrates the following situation: the rotor is axially displaced by a predetermined distance ΔX in a direction away from the nozzle guide vane 2. The magnitude of this displacement is chosen such that substantially all the flow from the end of the reaction zone travels toward the reactor outlet 9 (at a rotational speed U' > U).

[0119] Figure 4 B shows the flow at the design mass flow rate (where the flow enters the rotor at an absolute velocity V1, and the relevant streamlines are shown by dashed lines) and at the non-design mass flow rate V1. ’ The flow transport path below, in which the mass flow rate through the reactor increases (see streamline V1) ’ >V1). In both cases, the rotor rotational speed (U) is provided in the design mode. From Figure 4 It can be observed that with the increase of mass flow rate (V1) B, ’ Under these conditions, a portion of the flow is directly transferred from reactor inlet 8 to reactor outlet 9.

[0120] Figure 4 Figure C illustrates the following situation: where the rotor is axially displaced by a predetermined distance ΔX in the direction of the nozzle guide vane 2. The magnitude of this displacement is chosen such that substantially all of the flow travels from the reactor inlet 8 to the starting point of the reaction zone (at a mass flow rate V1). ’ >V1 (below).

[0121] Figure 5 Figure B shows the flow transport path at the design mass flow rate (where the flow enters the rotor at an absolute velocity V1, and the relevant streamlines are shown by dashed lines) and at the non-design mass flow rate, where the mass flow rate through the reactor decreases (see streamline V1). ’ <V1). In both cases, the rotor rotational speed (U) is provided in the design mode. From Figure 5 It can be observed from B that, with the decrease in mass flow rate V1 ’ Below, a portion of the flow is transferred from the end of the reaction zone back to the beginning of the reaction zone.

[0122] Figure 5 C illustrates the following situation: the rotor is axially displaced by a predetermined distance ΔX in the direction opposite to the nozzle guide vane 2. The magnitude of this displacement is chosen such that substantially all the flow travels from the end of the reaction zone toward the reactor outlet 9 (at a mass flow rate V1). ’ <V1 below).

[0123] like Figures 2 to 5 As shown in Figure C, the rotor is configured to be displaceable in the axial direction. This displacement of the entire rotor is achieved through a bearing mechanism described further below. The rotor displacement results in the associated rotor blades 3 being displaced by a preselected distance ΔX relative to the stationary reactor components.

[0124] The displacement distance of the exemplary device 100 can be configured to be 5mm-15mm (see also Example 1). However, it should be understood that the displacement distance in the axial direction can vary depending on the size, type, design and / or purpose of the reactor device.

[0125] Additional or alternative solutions may involve moving rotor disk 3A along rotor shaft 1 (not shown).

[0126] Reference Figures 2 to 5 In the described configuration, rotor 3 is configured to be axially displaceable in the direction of the stationary guide vane cascade (i.e., the nozzle guide vane cascade) located upstream of the rotor blade cascade. This is confirmed by positioning the movable bearing near the rotor drive unit. In the reactor described herein, a disk with associated blade cascades is positioned between the annular guide vane cascades; therefore, displacement of the rotor blade cascades toward any stationary cascade changes the original position of the rotor blades with respect to the two stator blade cascades. For clarity, the stationary guide vane cascades cannot be axially displaced.

[0127] Therefore, in some embodiments, the invention means adjusting the position of the rotor blade cascade 3 relative to the stationary guide vane cascade 2, 4 in a stator-rotor-stator arrangement by providing a rotor whose axial displacement by a predetermined distance (ΔX) in the longitudinal direction (X-X') of the rotor shaft is relative to the stationary guide vane cascade 2, 4 of the reactor (i.e., the stationary guide vane cascade 2, 4 and the housing 6).

[0128] In some configurations, when the rotor rotational speed (U) is reduced and / or the flow rate of the processed fluid through the reactor is increased, the rotor is shifted longitudinally by a predetermined distance (ΔX) toward the stationary guide vane cascade 2 located upstream of the rotor blade cascade 3. In practice, the modified flow rate refers to the modified mass flow rate caused by the increase in the consumption of raw material.

[0129] In some other configurations, when the rotor rotational speed is increased and / or when the flow rate of the processed fluid through the reactor is reduced, the rotor is displaced longitudinally by a predetermined distance (ΔX) away from the stationary guide vane cascade 2 located upstream of the rotor blade cascade 3. In practice, the modified flow rate refers to the modified mass flow rate caused by the reduction in the consumption of raw material.

[0130] In some embodiments, the distance along the rotor axis between the rotor blade cascade 3 and the stationary guide vane cascades 2 and 4 is adjusted by displacing (multiple) stationary components of the reactor along the rotor axis. The (multiple) stationary components are displaced a predetermined distance (ΔX) along the rotor axis 1 (in the direction X-X'). In this case, the rotor remains stationary. Alternatively, axial movement of the stationary components may accompany axial movement of the rotor.

[0131] As an example, when these components are connected to each other, the axial displacement of the housing 6 may be accompanied by the axial displacement of at least one stationary guide vane grating (e.g., nozzle guide vane grating 2).

[0132] For example, changing the position of the rotor blade cascade in the manner described above by translating the rotor and / or stationary components allows for high-precision adjustment of flow leakage. The quantity and / or direction (inlet to outlet, end of the reaction zone to the beginning of the adjacent reaction zone) can be effectively adjusted.

[0133] Changes in (mass) flow rate and associated feed consumption can be further compensated for by altering the feed-to-diluent ratio (e.g., where the diluent is (water) steam) so that the total flow rate of the feed-containing treatment fluid (i.e., the feed-diluent mixture) through the reactor remains constant.

[0134] For example, as described above, adjusting the position of the rotor blade cascade relative to the stationary guide vanes by axial displacement of the rotor can be achieved in reactor 100 set to an operating mode or a non-operating mode. In this context, "operating mode" refers to the state of equipment 100 resulting from its use or application, and optionally means setting the rotor to rotate. For example, such use may occur during normal operation (meaning the chemical reaction(s) taking place in the reaction) or during system testing. On the other hand, a non-operating mode typically means that equipment 100 is stopped or shut down.

[0135] When a reactor is to be adapted to feedstocks that are different from those previously used (e.g., different in terms of source and / or varying chemical composition), rotor shifting is typically performed in a reactor set to non-operating mode, as such adaptation may require additional adjustments to the system.

[0136] The rotor can be shifted to set the reactor to an operating mode. In this case, axial shifting can be performed manually or automatically, with automatic adjustment of the axial rotor movement achieved and controlled by a local or centralized control system (not shown). In some cases, axial shifting can be performed without stopping the rotor rotation. In this case, reducing the rotor rotation speed may be advantageous.

[0137] Similar considerations apply to the axial displacement of (multiple) stationary components.

[0138] Any combination of methods described above and designed to adjust for flow losses caused by leakage flowing in the circumferential direction can be used.

[0139] Further reference Figure 6A and Figure 6B ,in, Figure 6A A reactor 100 according to an embodiment is shown, and Figure 6B It shows the design along the line. Figure 6A The cross-sectional views are taken along lines AA and BB. The cross-sectional area along line AA is located at the inlet of the nozzle guide vane cascade 2, while the cross-sectional area along line BB is located at the outlet of the diffuser vane cascade 4. Overall, the cross-sections AA and BB depict the events occurring at the inlet and outlet of the stator-rotor-stator arrangement.

[0140] On the image depicting the transverse lines AA and BB ( Figure 6B The diagram indicates the locations where the processing streamlines enter and exit the reactor interior. Additionally, the processing streamlines that typically follow a helical path through stator-rotor-stator arrangements 2, 3, and 4 are indicated as individually numbered sector areas or sections (see Roman numerals i-vii). The right side shows a flow diagram illustrating the streamline channels through the reactor. Figure 6B Accordingly, the streamlines traveling between the first inlet 8A and the first outlet 9A are shown (the streamlines traveling between the second inlet 8B and the second outlet 9B are not shown).

[0141] In operation, the processing fluid containing the raw material enters the reactor through inlet opening 8 (here, 8A) and reaches the first stationary guide vane cascade 2 (nozzle-guided guide vane cascade). The inlet area within the first stationary guide vane cascade 2 is shaded on the cross-section AA. Figure 6B Some stationary guide vanes located in the inlet area are connected to the relevant inlet openings via (multiple) partitions, thereby forming a working chamber between the inlet and the outlet.

[0142] The fluid flow is delivered via the stator-rotor-stator arrangement 2, 3, 4, meaning that in practice the flow is delivered sequentially through the (stationary) nozzle guide vane 2, through the (rotating) rotor blades 3, and through the (stationary) diffuser guide vane 4; thereafter, the flow exits (multiple) vane cascades at sector (i) of the diffuser vane cascade (cross-section BB) and flows "upward" through the vaneless space 7. This flow enters the vaneless space after exiting the second stationary guide vane cascade 4 (diffuser guide vane cascade).

[0143] Each time the process fluid is conveyed through the stator-rotor-stator blade cascade, the temperature of the process flow increases, thus promoting (multiple) chemical reactions arranged in the vaneless space downstream of the cascade, as observed in the direction of fluid flow.

[0144] After passing through the vaneless space 7, the flow reaches sector (i) of the nozzle guide vane cascade 2 (cross-section AA) and repeats the above process. That is, the fluid flow generally follows a helical path through cascades 2, 3, and 4, exits at sector (ii) of the diffuser cascade 4 (cross-section BB), and continues through the vaneless space 7 toward sector (ii) of the nozzle guide vane cascade 2 (cross-section AA). Figure 6B In the configuration presented above, the flow is conveyed through the blade cascade eight (8) times (to establish 8 stages accordingly). After the last (here, the eighth) conveyance through the stator-rotor-stator blade cascade, the flow leaves the blade cascade and proceeds to the reactor outlet 9 (here, 9A).

[0145] On the transverse line BB, the exit area within the second stationary guide vane cascade 4 is shaded. Some stationary guide vanes located in the exit area are connected to the relevant exit openings via multiple partitions.

[0146] refer to Figures 8A to 8C It schematically shows the rotor ( Figure 8A , Figure 8B ) and (multiple) stationary parts Figure 8C Various arrangements of axial displacement.

[0147] In all basic embodiments, reactor 100 includes a (gas) casing 6 surrounding rotor blades 3 and annular stationary guide vane stacks 2, 4 disposed on both sides of the rotor. A flow forming device 5 in the form of a hollow ring is installed within the casing 6, thereby establishing an annular channel between the inner surface of the casing 6 and the outer surface of the flow forming device 5. The portion of the channel not occupied by blades / guide vanes forms a guide vane-free space 7.

[0148] Implementation as 100A ( Figure 8AThe reactor also includes at least one thrust bearing element 23 (which may also be referred to as a stop sliding bearing) arranged on the rotor shaft 1. The thrust bearings (multiple) support axial loads acting parallel to the shaft axis. The thrust bearing element 23 can be configured as a hydrodynamic thrust bearing, for example, in which a stop disc 23A is fitted between corresponding pads or races. Any other suitable configuration can be utilized.

[0149] The thrust bearing element 23 is configured to be displaceable along the rotor shaft 1 relative to stationary parts of the reactor (e.g., housing 6). Therefore, in Figure 8A In this configuration, the rotor is axially displaceable by the axial displacement of the thrust bearing element 23. In this configuration, the shaft coupling 1A arranged between the rotor shaft 1 and the drive shaft 1B is advantageously constructed as a flexible coupling, which allows either (or both) of the drive shaft and the rotor shaft to be axially displaced in the axial direction.

[0150] Figure 8B Configuration 100B is shown, in which the rotor is axially displaceable by axial movement of drive shaft 1B (the drive shaft is connected to rotor shaft 1 via coupling 1A). Coupling 1A can be rigid (preferred) or flexible. Reactor 100B can be implemented without thrust bearings(s).

[0151] In some specific configurations, reactor 100B is implemented without thrust bearings, drive shaft 1B is configured to be displaceable in the axial direction, and coupling 1A arranged between drive shaft 1B and rotor shaft 1 is non-flexible (in the axial direction), i.e., the coupling does not allow mutual displacement between drive shaft and rotor shaft.

[0152] Configuration 100A, 100B ( Figure 8A , Figure 8B The reactor is characterized by fixed, stationary components. In particular, the reactor shell is constructed to be stationary (non-displaceable) with respect to the reactor actuator 1C. In both configurations, reciprocating motion of the rotor in the axial direction is possible.

[0153] Configurations 100A and 100B may involve providing sliding radial bearings (journal bearings). Optionally, the sliding radial bearings are arranged longitudinally on the rotor shaft 1 in the relevant bearing housing on the opposite side of the rotor disk 3A (see details). Figure 9 (Description).

[0154] Figure 8CThe configuration (100C) is shown, in which the position of the rotor blade cascade 3 relative to the stationary guide vane cascades 2, 4 in the stator-rotor-stator arrangement can be adjusted by axially displacing at least one stationary component (particularly the reactor housing 6) in the longitudinal direction of the rotor shaft. Displacement of either the housing 6 and / or the stationary guide vane cascades 2, 4 can be adjusted by sliding the radial bearings 22, 32 (see [reference]). Figure 9 (Description).

[0155] Overall, reactor 100 can be implemented without thrust bearings 23 (e.g., configuration 100C).

[0156] In device 100C, drive shaft 1B is preferably fixed (non-displaceable) in the axial direction. Furthermore, coupling 1A is preferably constructed to be rigid (non-flexible) so that drive shaft 1B and rotor shaft 1 are non-displaceable in the axial direction.

[0157] In some specific configurations, reactor 100C is implemented without thrust bearings, drive shaft 1B is constructed to be immovable in the axial direction, and coupling 1A arranged between drive shaft 1B and rotor shaft 1 is also non-flexible, thereby preventing axial displacement of drive shaft and rotor shaft.

[0158] In this disclosure, the gas casing 6 is generally referred to as the reactor casing. However, the device structure 100 (100A, 100B, 100C) may be further enclosed in a separate outer casing (not shown).

[0159] refer to Figure 9 It illustrates an exemplary mechanism for axial rotor displacement in reactor 100, the mechanism involving the displacement of a thrust bearing. Overall, Figure 9 The configurations 100 and 100A shown are based on Figure 8A The configuration shown avoids repetition in describing the basic embodiment.

[0160] exist Figure 9 In this configuration, the reactor includes a bearing system comprising radial (sliding) bearing elements 22, 32 and at least one thrust bearing element 23. In some configurations, the radial bearing elements are journal bearings arranged longitudinally on opposite sides of the rotor disk 3A on the rotor shaft 1. The radial bearings support rotor loads acting perpendicular to the axis of the rotor shaft. Each radial bearing element 22, 32 is assembled in a housing 22A, 32A (radial bearing housing) and supported by a suitable O-ring seal 39 (not shown on the other side).

[0161] At least one thrust bearing 23 is arranged on the rotor shaft adjacent to the radial bearing. Any suitable radial (journal) bearing configuration and thrust bearing configuration can be used.

[0162] In some configurations, the bearing system thus implements a pair of radial bearings 22, 32, wherein the radial bearing element 22 and the thrust bearing element 23, arranged adjacently on the rotor shaft on one side of the rotor disk, are housed in a housing 21 and form a first bearing seat. The radial bearing element 32, arranged on the rotor shaft on the other side of the rotor disk, is housed in a housing 31 to form a second bearing seat. The bearing seats are mounted on both sides of the gas casing 6.

[0163] Preferably, the thrust bearing element is mounted on the rotor shaft near the rotor drive unit (i.e., on the side where the rotor disc is connected to the drive engine).

[0164] The bearing housing located at the front / inlet end of the reactor (i.e., at the end where the nozzle guide vane cascade 2 is arranged) is referred to as the first bearing housing, while the bearing housing located at the rear / outlet end of the reactor (i.e., at the end where the diffuser guide vane cascade 4 is arranged) is referred to as the second bearing housing. Each of the first and second bearing housings includes a bearing, optionally a bearing assembly, fitted into corresponding housings 21, 31 (bearing housing housings). The aforementioned bearing assembly is configured to absorb radial loads and advantageously also absorbs axial (thrust) loads.

[0165] exist Figure 9 In the device, the thrust bearing element 23 is housed in a separate housing 24 (thrust bearing housing), which is at least partially surrounded within the housing 21 of the associated bearing seat. An end seal 29 (rotor shaft) is mounted in the thrust bearing housing 24 below the thrust bearing housing cover 24A.

[0166] Alternatively or additionally, the thrust bearing may be housed in a second bearing housing (not shown).

[0167] Lubricating oil is supplied from an oil system (not shown) to the bearing housing via corresponding oil inlet passages 25 and 35 in the bearing housing housings 21 and 31. Oil is discharged from the bearing through oil outlet passages 26 and 36. Separate oil passages (inlet and outlet) are arranged in the thrust bearing housing 24 for lubricating and cooling the thrust bearing housing.

[0168] The bearing housing may also include labyrinth seals 27, 37. To avoid contamination of the processed fluid and / or overheating during processing, liquid-free labyrinth seals, such as gas labyrinth seals, can be used. For example, steam (water vapor) or inert gases (such as nitrogen) can be used to provide the seal. The inert gas is supplied to the labyrinth seal through channels 28, 38.

[0169] In some configurations, each of the stationary guide vane cascades 2, 4, and optionally the housing 6, is fixed to the bearing housing.

[0170] The thrust bearing element 23, enclosed (24), is configured to be axially displaced a predetermined distance ΔX in the longitudinal direction of the rotor shaft (along axis X-X') within the associated bearing housing. The thrust bearing 23 is displaced relative to the housing 21 of the bearing housing. Due to its displaceability relative to the bearing housing housing, the thrust bearing element 23 can also be displaced relative to stationary parts of the reactor (e.g., the outer casing 6).

[0171] As described above, the rotational motion of the rotor is supported by radial bearings 22 and 32 mounted along the rotor shaft 1. On the other hand, the thrust bearing element 23 allows the rotor to be axially displaced.

[0172] Therefore, in Figure 9 In this embodiment, by adjusting the position of the thrust bearing element 23 enclosed (24) in the relevant bearing housing in the longitudinal direction of the rotor shaft relative to the housing 21 of the bearing housing, the rotor can be axially displaced relative to the stationary guide vane grates 2, 4 and relative to the gas casing 6. Therefore, reciprocating motion of the rotor in the axial direction can be achieved.

[0173] Device 100 can be implemented according to the following example.

[0174] Example 1. The device 100 includes a gas casing 6 with two inlets 8A, 8B and two outlets 9A, 9B. The casing surrounds a rotor 3 and annular stationary guide vane grates 2, 4 fixed to both sides of the rotor. A flow-forming device 5 in the form of a hollow ring hoop is installed within the casing, thereby forming an annular conduit, wherein the portion of the conduit not occupied by blades / guide vanes forms a guide vane-free space 7. The rotor is configured to be displaceable along the longitudinal axis X-X'. The reactor 100 operates with the parameters defined in Table 2.

[0175] Table 2 Exemplary parameters related to rotor blade cascade 3 and the processed fluid flow.

[0176]

[0177] In the device 100 designed and implemented according to the parameters in Table 2, in order to avoid or at least minimize circumferential flow leakage caused by a 25% reduction in rotational speed U, the rotor must be axially displaced by a distance ΔX equal to 6.6 mm in the direction of the nozzle guide vane grating.

[0178] Figure 7 The effect of this shift is further illustrated, where Figure 7 Figure A shows the velocity triangles (values ​​given in millimeters) achievable in reactor 100 according to the design parameters in Table 2.

[0179] Figure 7Figure B shows the velocity triangle under non-design operating conditions involving a 25% reduction in rotational speed U' compared to the rotational speed U in design mode. Velocities W1 and V2 are indicated by dashed arrows.

[0180] Figure 7 Figure C illustrates the following situation: where the rotor blade 3 is displaced by a distance ΔX in the direction of the nozzle guide vane 2. In the current case, ΔX = 6.6 mm. With the selected displacement amplitude, virtually all the flow entering the reactor is forced into the starting point of the reaction zone.

[0181] The device 100, constructed using the blade parameters according to Table 2, also comprises... Figure 9 As shown. Note that the shift distance ΔX constitutes 8 mm. Where applicable, the values ​​on (multiple) graphs are given in millimeters.

[0182] In a non-limiting manner, in all the configurations described above, the rotor's peripheral (rotational) speed (U) can be set in the range of 150 m / s to 400 m / s. The speed depends on how much energy needs to be supplied to the processing stream for a given raw material composition.

[0183] The axial dimensions of the rotor blades can be set within the range of 20mm-90mm. The axial clearance between the nozzle guide vane cascade and the rotor blade cascade can be set within the range of 6mm-40mm. Overall, the dimensions of the rotor blades and stationary guide vanes, as well as the clearance between them, depend accordingly on the dimensions of the reactor 100 and its performance capabilities.

[0184] The displacement distance ΔX in a reactor with the above specifications can vary in the range of approximately 0.5 mm to 25 mm; this range can be extended when the device is expanded.

[0185] A reactor arrangement (not shown) can be established when at least two reactor devices 100 are connected in parallel or series. The connection between the devices can be mechanical and / or functional. A functional (e.g., chemical) connection can be established when at least two separate, physically integrated or non-integrated reactors 100 are associated. In the case of non-integrated reactors, the association between the at least two devices 100 can be established via multiple auxiliary facilities (not shown). In some configurations, the arrangement includes at least two devices that are functionally connected at least via their central axes. This configuration can be further defined as at least two devices 100 having a series (sequential) mechanical connection, while a functional (e.g., in terms of feedstock-based reactions) connection can be considered as a parallel (array) connection.

[0186] In some cases, the arrangement may also include a preheating furnace (here, a furnace). The furnace and at least one reactor 100 may together form a cracker unit (not shown). Multiple reactors 100 in parallel may be connected to a common furnace; or multiple reactors 100 may be connected to multiple furnaces.

[0187] On the other hand, the equipment 100 and / or related arrangements are provided for use in the thermal or thermochemical conversion of hydrocarbon feedstocks.

[0188] In the selected configuration, the conversion is the thermal or thermochemical cracking of the hydrocarbon feedstock, particularly the fluidized hydrocarbon feedstock (i.e., fluidized organic feedstock material mainly containing carbon and hydrogen).

[0189] Additionally or alternatively, reactor 100 may be configured to process oxygen-containing feedstocks, such as oxygenated hydrocarbon derivatives. In some configurations, reactor 100 may be adapted to process cellulose-based feedstocks. In some additional or alternative configurations, reactor 100 may be adapted to process feedstocks based on (waste) animal fats and / or (waste) vegetable oils. Pretreatment of the animal fat and vegetable oil-based feedstocks may include hydrogenation deoxygenation (removal of oxygen from oxygenated compounds), which causes the (tri)glycerol ester structure to decompose and primarily produce straight-chain alkanes. In further additional or alternative configurations, reactor 100 may be adapted to process byproducts of the wood pulp industry, such as tail oil or any derivative thereof. "Tail oil" is defined as a well-known byproduct of the sulfate process used primarily in the pulping of coniferous trees in wood pulp production.

[0190] In this process, the hydrocarbon feedstock is provided as, but not limited to, any of the following: medium-weight hydrocarbons (such as naphtha and gas oil) and light hydrocarbons (such as ethane, propane, and butane). Propane and heavier fractions may be further utilized.

[0191] In some cases, the hydrocarbon-containing feedstock is gasified pretreated biomass material. Biomass-based feedstocks are cellulose-derived or particularly lignocellulose-derived pretreated biomass supplied to the reactor in a substantially gaseous form.

[0192] Hydrocarbon-containing feedstocks can also be provided as any of the following: pretreated glycerol-based materials (such as (waste or residual) vegetable oils and / or animal fats) or pretreated plastic waste or residues. As mentioned above, the pretreatment of the (tri)glycerol-based feedstocks can include various treatments, such as pyrolysis or deoxidation. A range of plastic wastes comprising PVC, PE, PP, PS materials and mixtures thereof can be used in treatments to recover pyrolysis oils or gases, which can also be used as feedstocks for the production of new plastics and / or refining into (various) fuel oils (diesel equivalents).

[0193] Therefore, in the selected embodiments, reactor 100 can be configured to perform at least one process selected from the group consisting of: processing a hydrocarbon feedstock preferably containing medium-weight and light hydrocarbon fractions; processing a gasified carbohydrate-containing feedstock; processing a gasified feedstock containing glycerides and / or fatty acids; and processing a gasified cellulosic biomass material. Thus, reactor 100 can be configured to process oxygenated feedstock materials, for example, those derived from bio-based feedstocks. Possible applications include the refining of biomass-based or biomass-derived substances to produce renewable fuels in processes such as the direct catalytic hydrogenation of vegetable oils or animal fats to the corresponding alkanes or gaseous hydrocarbons as a stage of the Fischer-Tropsch process. Additionally, the reactor can be configured for the enhancement (refining or strengthening of gaseous substances) of bio-based pyrolysis gases or syngas.

[0194] When using feedstocks based on biomass, glycerides, and / or polymers, reactor 100 can also be adapted for catalytic treatment. This is achieved by contacting multiple catalytic surfaces (not shown) formed by multiple catalytic coatings on the reactor blades or inner walls with multiple treatment fluids. In some cases, the reactor may include multiple catalytic modules defined by multiple ceramic or metal substrates or support carriers having active (catalytic) coatings, which may optionally be implemented as an integral honeycomb structure.

[0195] On the other hand, a method is provided for improving processing efficiency and adjusting flow losses during the processing of feedstock in a processing fluid, the method comprising at least the following steps:

[0196] a. Obtain device 100, which includes:

[0197] - Rotor, the rotor includes multiple rotor blades arranged in the circumferential direction of a disk (3a) mounted on a rotor shaft (1) and forming a rotor blade cascade (3);

[0198] - Multiple stationary guide vanes, arranged in an annular guide vane cascade (2, 4), are arranged adjacent to the rotor blade cascade, thus forming a stator-rotor-stator arrangement (2, 3, 4); and

[0199] - A housing (6) in which a pipe is formed, the pipe having at least one inlet (8) and at least one outlet (9), the housing enclosing the rotor blade cascade (3) and the stationary guide vane cascade (2, 4) inside the pipe;

[0200] as well as

[0201] b. Adjust the position of the rotor blade cascade in the stator-rotor-stator arrangement relative to the stationary guide vane cascade by a predetermined distance (ΔX) along the rotor shaft in the axial direction.

[0202] This method is particularly advantageous for operating equipment 100 under non-design conditions.

[0203] In this method, the position of the rotor blade cascade relative to the stationary guide vane cascade in the stator-rotor-stator arrangement is adjusted by axially displacing the rotor in the longitudinal direction of the rotor shaft. Alternatively, the stationary component (e.g., the housing) can be displaced. Reciprocating motion of either the rotor or the stationary component along the rotor shaft in the longitudinal direction can be achieved.

[0204] In some embodiments, adjusting the position of the rotor blade cascades relative to the stationary guide vane cascades in the stator-rotor-stator arrangement involves at least adjusting the rotor's rotational speed and / or the flow rate of the processing fluid containing the raw material. In some cases, adjusting the flow rate includes adjusting the mass flow rate indicating the total consumption of the raw material.

[0205] In some embodiments, when the rotational speed of the rotor is reduced and / or when the flow rate of the processed fluid through the reactor 100 is increased, the rotor is displaced in the longitudinal direction by a predetermined distance ΔX toward the stationary guide vane 2 (nozzle guide vane 3) disposed upstream of the rotor blade cascade 3.

[0206] In some other embodiments, when the rotational speed of the rotor is increased and / or when the flow rate of the processed fluid through the reactor 100 is reduced, the rotor is displaced a predetermined distance ΔX in the longitudinal direction away from the stationary guide vane cascade 2 located upstream of the rotor blade cascade 3.

[0207] In this method, the position of the rotor and / or stationary components can be adjusted in a device set to operating mode or non-operating mode.

[0208] In this method, the feedstock advantageously includes hydrocarbons. In some cases, the feedstock includes at least one alkane feed (ethane, propane, butane), naphtha feed, gas oil, and / or any other feedstock suitable for producing substantially low molecular weight unsaturated hydrocarbons, preferably such as olefins (ethylene, propylene, butene), and acetylene.

[0209] Those skilled in the art will understand that, with advancements in technology, the basic idea of ​​this invention can be implemented in various ways. The invention and its embodiments can generally be varied within the scope of the appended claims.

Claims

1. An apparatus for processing raw materials in a processing fluid, comprising: - A rotor comprising a plurality of rotor blades arranged circumferentially on a disk (3a) mounted to a rotor shaft (1) and forming a rotor blade cascade (3). - Multiple stationary guide vanes, which are arranged in an annular arrangement of multiple stationary guide vane cascades, which are disposed adjacent to the rotor blade cascades to form a stator-rotor-stator arrangement. - A housing (6) having a conduit formed therein, the conduit having at least one inlet (8) and at least one outlet (9), the housing enclosing the rotor blade cascade (3) and the stationary guide vane cascade inside the conduit, and - A guide vane-less space (7) is formed between the outlet of the stator-rotor-stator arrangement and the inlet of the stator-rotor-stator arrangement. In the stator-rotor-stator arrangement, the stationary guide vane cascade and the rotor blade cascade are configured to guide the processing fluid through the stationary guide vane cascade and the rotor blade cascade according to a helical flow path and through the guide vaneless space (7) as it is conveyed in the pipe between the at least one inlet and the at least one outlet, and are configured to establish conditions for at least one chemical reaction to occur in the processing fluid. In the stator-rotor-stator arrangement, the position of the rotor blade cascade (3) relative to the stationary guide vane cascade can be adjusted by a predetermined distance (ΔX) along the rotor axis in the axial direction.

2. The device according to claim 1, wherein, The position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade can be adjusted by axially shifting the rotor in the longitudinal direction of the rotor shaft.

3. The device according to any one of claims 1 and 2, further comprising at least one thrust bearing element (23) disposed on the rotor shaft, wherein, The rotor can be axially displaced by axial displacement of the at least one thrust bearing element on the rotor shaft.

4. The device according to claim 3, wherein, The at least one thrust bearing element (23) is configured to be axially displaced relative to the housing (6).

5. The device according to claim 3, wherein, The thrust bearing element (23) is housed in a separate housing (24), which is at least partially surrounded inside a bearing housing (21), wherein the surrounded thrust bearing element (23) is configured to be axially displaced in the longitudinal direction of the rotor shaft within the associated bearing housing.

6. The device according to any one of claims 1 and 2, wherein, The coupling (1A) arranged between the rotor shaft (1) and the drive shaft (1B) is a flexible shaft coupling, which is configured to allow the drive shaft and the rotor shaft to be axially displaced.

7. The device according to claim 6, wherein, The rotor can be axially displaced by the axial displacement of the drive shaft (1B) connected to the rotor shaft (1) via the coupling (1A).

8. The device according to claim 6, wherein, The position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade can be adjusted by axially shifting the housing (6) in the longitudinal direction of the rotor shaft.

9. The device according to claim 8, wherein, The drive shaft (1B) is fixed, thereby preventing axial displacement of the drive shaft.

10. The device according to any one of claims 7 to 9, wherein, The coupling (1A) is a rigid coupling, which is configured to prevent the drive shaft and the rotor shaft from shifting axially.

11. The device according to any one of claims 1 and 2, wherein, Each of the plurality of stationary guide vane grates is fixed on a corresponding bearing seat arranged on both sides of the housing (6).

12. The device according to any one of claims 1 and 2, wherein, Adjusting the position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is accompanied by at least adjusting the rotational speed of the rotor and / or the flow rate of the processing fluid containing the raw material.

13. The device according to any one of claims 1 and 2 further includes a flow forming device (5) disposed inside the housing (6) such that the conduit is formed between the housing and the flow forming device, the conduit having an annular meridional cross section.

14. The device according to claim 13, wherein, The flow forming device (5) is an annular hollow structure.

15. The device according to claim 14, wherein, The vaneless space (7) formed between the outlet of the stator-rotor-stator arrangement and the inlet of the stator-rotor-stator arrangement is defined by the volume portion between the housing (6) and the flow forming device (5).

16. The device according to any one of claims 1 and 2, wherein, The stationary guide vane cascade has multiple stationary nozzle guide vanes and multiple stationary diffuser guide vanes. The multiple stationary nozzle guide vanes form an annular nozzle guide vane cascade upstream of the rotor blade, and the multiple stationary diffuser guide vanes form a diffuser guide vane cascade downstream of the rotor blade.

17. The device according to any one of claims 1 and 2, wherein the device is configured with a plurality of catalytic surfaces.

18. The use of the equipment according to any one of claims 1 to 17, for heat treatment of hydrocarbon-containing feedstocks.

19. The use of the apparatus according to any one of claims 1 to 17, for carrying out a chemical reaction.

20. The use according to claim 19, for thermochemical cracking of hydrocarbon-containing feedstocks.

21. The use according to claim 19, for performing at least one step selected from the group consisting of: processing a hydrocarbon feedstock containing medium-weight hydrocarbon and light hydrocarbon fractions, wherein the medium-weight hydrocarbons are selected from naphtha and gas oil, and the light hydrocarbons are selected from ethane, propane, and butane; processing a vaporized carbohydrate-containing feedstock; and processing a vaporized feedstock containing glycerides and / or fatty acids.

22. The use according to claim 21, wherein, The gasified carbohydrate-containing raw material is gasified cellulose biomass material.

23. An arrangement for processing raw materials, comprising at least two devices according to any one of claims 1 to 17, wherein the at least two devices are connected in parallel or in series.

24. A method for improving treatment efficiency and adjusting flow losses under non-design conditions during the treatment of a feedstock in a process fluid, comprising: a. Obtaining equipment, said equipment comprising: - A rotor comprising a plurality of rotor blades arranged circumferentially on a disk (3a) mounted to a rotor shaft (1) and forming a rotor blade cascade (3). - Multiple stationary guide vanes, which are arranged in multiple annular stationary guide vane cascades, which are arranged adjacent to the rotor blade cascades to form a stator-rotor-stator arrangement. - A housing (6) in which a conduit is formed, the conduit having at least one inlet (8) and at least one outlet (9), the housing enclosing the rotor blade cascade (3) and the stationary guide vane cascade inside the conduit, and - A guide vane-less space (7) is formed between the outlet of the stator-rotor-stator arrangement and the inlet of the stator-rotor-stator arrangement. The stationary guide vane cascade and the rotor blade cascade in the stator-rotor-stator arrangement are configured to guide the processing fluid through the stationary guide vane cascade and the rotor blade cascade and through the guide vaneless space (7) according to a helical flow path as it is conveyed in the pipe between the at least one inlet and the at least one outlet, and are configured to establish conditions for at least one chemical reaction to occur in the processing fluid; as well as b. Adjust the position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade in the axial direction along the rotor axis by a predetermined distance (ΔX).

25. The method according to claim 24, wherein, The position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is adjusted by axially shifting the rotor in the longitudinal direction of the rotor shaft.

26. The method according to claim 24, wherein, The position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is adjusted by axially shifting the housing (6) in the longitudinal direction of the rotor shaft.

27. The method according to any one of claims 24 to 26, wherein, Adjusting the position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is accompanied by at least adjusting the rotational speed of the rotor and / or the flow rate of the processing fluid containing the raw material.

28. The method according to any one of claims 24 and 25, wherein, When the rotational speed of the rotor is reduced and / or when the flow rate of the processed fluid through the device is increased, the rotor is shifted in the longitudinal direction by a predetermined distance (ΔX) toward the stationary guide vane cascade (2) disposed upstream of the rotor blade cascade (3).

29. The method according to any one of claims 24 and 25, wherein, When the rotational speed of the rotor is increased and / or when the flow rate of the processed fluid through the device is reduced, the rotor is displaced by a predetermined distance (ΔX) in the longitudinal direction away from the stationary guide vane cascade (2) located upstream of the rotor blade cascade (3).

30. The method according to any one of claims 24 to 26, wherein, Adjusting the position of the rotor blade cascade (3) in the stator-rotor-stator arrangement relative to the stationary guide vane cascade is performed in the device when it is set to an operating mode or a non-operating mode.

31. The method according to any one of claims 24 to 26, wherein, The raw materials include hydrocarbons.

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