Rotary feed material processing device with axially adjustable rotor

Abstract

A rotating bladed apparatus 100 for processing a feedstock in a process fluid is provided, the apparatus 100 including means for adjusting the position of the working blade cascades of the rotor relative to a stator component in the longitudinal direction of the rotor shaft. The adjustment is made via axial displacement of the rotor or via axial displacement of the reactor housing. Methods are also provided for improving process efficiency and adjusting flow losses during processing of the feedstock in the process fluid, particularly at off-design conditions within the bladed apparatus 100. In an embodiment, the processing of the feedstock comprises thermal or thermochemical cracking of a hydrocarbon-containing feedstock.

Description

Technical Field

[0001] The present invention generally relates to the field of rotary turbomachines having axially adjustable rotors. In particular, the present invention relates to devices with rotating blades for processing feedstocks such as hydrocarbons, related configurations, methods, and uses.

Background Art

[0002] In the field of turbomachines, there are various solutions for making the rotor unit axially displaceable. These solutions are typically applicable in axial flow turbomachines such as axial flow compressors and turbines, and the radial flow losses can be efficiently adjusted by the axial displacement of the rotor. In an annular turbine cascade that uses a working fluid to rotate the rotor, a clearance gap is provided between the rotating parts and the stationary parts, so radial flow losses generally occur, which typically results in leakage paths (tip leakage).

[0003] As an example, DE 101 45 785 A1 (German Patent Application Publication No. 10145785) (Ehrenberger) discloses a wind turbine in which when the nominal speed of the rotor is exceeded, the rotor is axially shifted from its operating position to a lower speed position (in the direction of increasing the clearance between the rotor blades and the casing). The axial adjustment solves the problem of stabilizing the speed (rotational speed) of the rotor under conditions of variable fluid flow velocity of the incoming 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-flow reactor configured to hydrogenate dry coal to produce hydrocarbons, with a rotor configured to be axially displaced, is shown in U.S. Patent Publication No. 4,288,405 (Koch). The rotor is axially displaced when the pressure in the hydrogenation chamber exceeds a certain value. The movement of the rotor causes the feed port to the hydrogenation chamber to close, thereby preventing very high pressures from spreading to upstream equipment.

[0005] U.S. Patent Publications 9,494,038 (Bushuev) and 9,234,140 (Seppala et al.) disclose a rotodynamic reactor (RDR) apparatus for converting hydrocarbon feedstocks into light olefins via thermal (chemical) decomposition. Overall, the reactor comprises a rotor disk having an associated blade cascade surrounded within a casing provided in a toroidal shape, positioned between rows of stationary vanes arranged on an essentially ring-shaped support. The process fluid enters the reaction through an inlet and passes through the stator cascade and rotor cascade several times along an essentially helical trajectory before exiting the reactor.

[0006] Low molecular weight olefins such as ethylene, propylene, and butylene are major components of the petrochemical industry and play a fundamental role as building blocks in the commercial production of plastics, polymers, elastomers, rubber, foams, solvents, and chemical intermediates, as well as fibers (including carbon fibers) and coatings. Compared to conventional tubular pyrolysis furnaces, the rotodynamic machines described above enable thermal (chemical) reactions with shortened residence times and improved controllability of the decomposition process, the latter generally associated with preventing the products from entering secondary reactions and improving the yield of the desired product.

[0007] A common problem with the aforementioned known RDR solutions is the occurrence of flow leakage along the circumferential direction (also called the tangential or hoop direction). In practice, leakage occurs in the direction from the inlet to the outlet (without entering the reaction zone) and / or from the end of one reaction zone to the beginning of an adjacent reaction zone (without leaving the reactor), and such leakage is caused by operating the reactor under conditions different from the nominal conditions (so-called out-of-design modes).

[0008] For completeness, please note that leakage issues in the directions indicated above (from inlet to outlet, from the end of one reaction zone to the beginning of an adjacent reaction zone) are not observed in conventional axial flow solutions.

[0009] Therefore, when operating a reactor with variable flow rates and / or feedstock-related conditions, leakage is inevitable. Similarly, leakage occurs when changing the temperature inside the reactor (while all other parameters are constant) in relation to adjusting the rotor rotation speed.

[0010] Such leakage causes a reduction in total mass flow rate and work transfer, negatively impacting the reactor's stability and limiting its operating range, i.e., its ability to operate across a range of fluid flow rates and rotational speeds. Furthermore, flow leakage causes coke formation, significantly reducing the yield of the desired product. Therefore, flow leakage negatively impacts 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 apparatus with a single combination of mass flow rate through the reactor and rotor rotation speed, so that a specific predetermined rotation speed is assigned to a specific mass flow rate, provided that the composition of the feedstock does not change.

[0012] The solution proposed by Bushueff in U.S. Patent No. 9,494,038 (B2) suggests adjusting the geometric shape of the stationary vane cascade circumferentially when the reactor is operating under nominal design conditions to achieve pressure equalization across the entire blade cascade at the inlet to and outlet from the rotor blade cascade. In addition, the position of the stator vane cascade can be adjusted, but only circumferentially with respect to the rotor rotation axis. The above configuration aims to mitigate undesirable large-scale mixing between adjacent flows. However, this document does not address the problem of reducing leakage in off-design operating modes.

[0013] In this regard, updates are still needed in the field of improving the efficiency of rotary reactors (particularly RDR type reactors) for the chemical processing of hydrocarbon feedstocks, from the perspective of addressing challenges related to preventing or at least minimizing flow leaks in order to optimize the operating range and efficiency of reactors under variable process conditions. [Overview of the project]

[0014] The object of the present invention is to solve, or at least mitigate, any of the problems arising from the limitations and drawbacks of the related technology. The above object is achieved by various embodiments of apparatus, related configurations, methods and uses for processing feedstock in a process fluid. Accordingly, in one aspect of the present invention, an apparatus for processing feedstock in a process fluid is provided in accordance with the content defined in independent claim 1.

[0015] In one embodiment, the device comprises a rotor having a plurality of rotor blades arranged around the circumference of a disk mounted on a rotor shaft and forming a rotor blade cascade; a plurality of stationary vanes arranged in an essentially annular vane cascade adjacent to the rotor blade cascade to form a stator-rotor-stator array; and a casing that surrounds the rotor blade cascade and the stationary vane cascade within a duct having at least one inlet and at least one outlet, wherein the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator array is adjustable axially by a predetermined distance (ΔX) along the rotor shaft.

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

[0017] In one embodiment, the apparatus further comprises at least one thrust bearing element positioned on a rotor shaft, and the rotor is made axially displaceable by the axial displacement of the at least one thrust bearing element on the rotor shaft.

[0018] In one embodiment, the at least one thrust bearing element is configured to be displaceable in the axial direction relative to the (reactor) casing.

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

[0020] In one embodiment, the coupling positioned between the rotor shaft and the drive shaft is a flexible shaft coupling configured to allow axial displacement of the drive shaft and / or rotor shaft. Thus, the flexible coupling enables axial displacement of the drive shaft and / or rotor shaft.

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

[0022] In some embodiments, the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator array can be adjusted by axially displacing at least one stationary component, particularly the (reactor) casing, in the longitudinal direction of the rotor shaft. The drive shaft is preferably fixed so as to prevent its axial displacement.

[0023] In some further embodiments, the coupling positioned between the rotor shaft and the drive shaft is a rigid coupling configured to prevent axial displacement of the drive shaft and the rotor shaft.

[0024] In one embodiment, each of the stationary vane cascades is fixed on associated bearing blocks located on either side of the reactor (gas) casing.

[0025] In one embodiment, the apparatus is configured such that adjusting the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator array is accompanied by adjusting at least the rotational speed of the rotor and / or the flow rate of the feed material-containing process fluid.

[0026] In one embodiment, the device further comprises a rectifier disposed within the (gas) casing such that a duct is formed between the outer casing, and the duct has an annular meridional cross-section. In one embodiment, the rectifier is annular and has an essentially hollow structure.

[0027] In one embodiment, in the device, a vaneless space is formed between an exit from the stator-rotor-stator arrangement and an entrance to the stator-rotor-stator arrangement, and the vaneless space is defined by a volume between the (gas) casing and the rectifier.

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

[0029] In one embodiment, the cascade within the stator-rotor-stator arrangement is configured to direct a process fluid so that the process fluid repeatedly passes through the cascade and the vaneless space following a spiral flow path while propagating within a duct between at least one inlet and at least one outlet, establishing conditions under which at least one chemical reaction occurs within the process fluid.

[0030] In one embodiment, the device further comprises a plurality of catalyst surfaces.

[0031] In some other aspects, there is provided the use of the device for treating a feedstock in a process fluid according to the definitions in independent claims 19, 20. In one embodiment, the use is carried out in the heat treatment of a hydrocarbon-containing feedstock(s). Additionally or alternatively, the use is carried out to effect a chemical reaction. In one embodiment, the use is carried out for the thermal cracking or thermochemical cracking of a hydrocarbon-containing feedstock.

[0032] In one embodiment, the use is performed to carry out at least one procedure selected from the group consisting of processing hydrocarbon feedstocks preferably containing medium and light hydrocarbon fractions, processing feedstock materials containing gaseous carbohydrates, processing feedstock materials containing gaseous glycerides and / or fatty acids, and processing gaseous cellulosic biomass materials.

[0033] In another embodiment, a configuration of the apparatus for processing a feedstock in a process fluid according to the embodiment is provided, as defined in independent claim 23. In this configuration, at least two apparatuses are connected at least functionally in parallel or in series.

[0034] In yet another embodiment, a method is provided to improve process efficiency and adjust flow losses during processing of feedstock in a process fluid, as defined in independent claim 24. In one embodiment, the method is - A step of obtaining an apparatus comprising: a rotor having a plurality of rotor blades arranged around the circumference of a disk mounted on a rotor shaft and forming a rotor blade cascade; a plurality of stationary vanes arranged in an essentially annular vane cascade adjacent to the rotor blade cascade so as to form a stator-rotor-stator array; and a casing that surrounds the rotor blade cascade and the stationary vane cascade within a duct having at least one inlet and at least one outlet; - The step of adjusting the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator arrangement by a predetermined distance (ΔX) along the rotor shaft in the axial direction.

[0035] In one embodiment, the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator arrangement is adjusted by axially displacing the rotor in the longitudinal direction of the rotor shaft.

[0036] In another embodiment, the position of the rotor blade cascade relative to the stationary vane cascade in a stator-rotor-stator array is adjusted by axially displacing at least one stationary component, particularly the casing, in the longitudinal direction of the rotor shaft.

[0037] The usefulness of the present invention arises for various reasons depending on each specific embodiment. By providing a rotor that is displaceable axially (i.e., along the longitudinal direction of the rotor shaft), flow losses associated with tip clearance leaks, which are characteristic of known rotary reactors and / or turbomachinery, can be effectively prevented or at least minimized. In conventional rotary reactors, flow leaks trigger various secondary reactions that lead to the formation of by-products such as coke, reducing the yield of the primary (intended) product.

[0038] The present invention has proven particularly useful when attempting to operate a rotary reactor designed to carry out (thermal) chemical reactions, such as the (steam) decomposition of hydrocarbons, in an out-of-design mode established when changing a range of parameters within the reactor (e.g., process temperature, which is often related to the adjustment of the rotor rotation speed and / or the chemical composition of the feedstock). The solutions provided herein may be essential for use, for example, in decomposition equipment or any other related equipment operating with various feedstocks.

[0039] By utilizing a displaceable rotor solution, the operation of conventional rotary reactors can be optimized, at least in terms of efficiency, for multiple operating conditions different from those assigned to the design model. This thus expands the operating range of the reactor and associated equipment (e.g., disassembly equipment).

[0040] Rotor displacement solutions are flexible solutions and can be efficiently utilized in equipment designed for (thermal)chemical feedstock processing (RDR solutions, axial flow solutions, etc.), as well as in rotary turbomachinery.

[0041] The terms “pyrolysis” and “decomposition” are used in this disclosure primarily as synonyms for the process of pyrolysis of heavier hydrocarbon-containing compounds into lighter hydrocarbon-containing compounds.

[0042] In this specification, the expression "several" refers to any positive integer starting from 1, for example, 1, 2, or 3. In this specification, the expression "multiple" refers to any positive integer starting from 2, for example, 2, 3, or 4.

[0043] The terms “first” and “second” are used herein to distinguish one element from another, unless expressly otherwise specified, and not to indicate a particular order or importance.

[0044] In this disclosure, the terms “fluid” and “process fluid” primarily refer to gaseous feedstock flows guided through the interior of a reactor, for example, in the presence of a diluent.

[0045] The term "gasified" is used herein to indicate that a substance has been converted into a gaseous state by any possible means.

[0046] The term "hydrodynamic" is used herein to describe the dynamics of fluids, primarily represented by gases. Therefore, in this disclosure, the term is used as a synonym for "gaseous."

[0047] Different embodiments of the present invention will become apparent from the detailed description and accompanying drawings. [Brief explanation of the drawing]

[0048] [Figure 1] This figure shows the stator-rotor-stator array within device 100 operating under design conditions. [Figure 2-5]This figure shows the velocity triangle and stator-rotor-stator arrangement in a device 100 according to an embodiment, which operates at least partially under non-design conditions and in which the rotor is displaced by a predetermined distance ΔX relative to the stator elements. [Figure 6A] This is a vertical cross-sectional view of the apparatus 100 according to one embodiment. [Figure 6B] Figure 6A is a cross-sectional view along lines AA and BB shown, and is a flow diagram of the streamlined passages through the device 100. [Figure 7] This figure shows the velocity triangle and stator-rotor-stator arrangement in a device 100 that operates under design conditions and non-design conditions, where the rotor is displaced by a predetermined distance ΔX relative to the stator elements, according to one embodiment. [Figures 8A-8C] This figure shows different arrangements for axial rotor displacement according to an embodiment. [Figure 9] This is a vertical cross-sectional view of apparatus 100, which shows an exemplary mechanism for axial rotor displacement. [Modes for carrying out the invention]

[0049] Detailed embodiments of the present invention are disclosed herein with reference to the accompanying drawings. The same reference numerals are used throughout the drawings to indicate the same components.

[0050] Figure 6A shows a fundamental concept representing various embodiments of a reactor (hereinafter referred to as a reactor) for processing feedstock in a process fluid (working fluid), indicated by 100. Figures 8A to 8C and 9 show reactors 100 (100A, 100B, and 100C) according to this embodiment.

[0051] The implementation of apparatus 100 generally follows the guidelines set forth in U.S. Patent Publication No. 9,494,038 (Bushuev) and No. 9,234,140 (Seppara et al.). These patents, incorporated herein by reference, describe rotary turbomechanical reactors in which both the rotor and stator structures are essentially enclosed within a toroidal housing.

[0052] The reactor 100 is preferably configured to process a feedstock, such as a hydrocarbon-containing feedstock, by carrying out at least one chemical reaction in the process fluid, after which the feedstock is converted into a desired product.

[0053] In selected configurations, the reactor is configured for the thermal or thermochemical conversion of hydrocarbon-containing feedstocks, particularly fluid hydrocarbon-containing feedstocks. In this specification, “hydrocarbon-containing feedstocks” refers primarily to fluid organic feedstock materials containing carbon and hydrogen. However, in some examples, the reactor may be configured to process oxygen-containing feedstock materials such as oxygen-containing hydrocarbon derivatives, cellulosic feedstocks, and / or vegetable oil-based feedstocks. Therefore, the availability of the reactors proposed herein extends beyond the limitations set forth in the conventional definition of hydrocarbon feedstocks.

[0054] The hydrocarbon-containing feed flowing into the reactor is provided in an essentially fluid state, such as a liquid or a gas. In a preferred embodiment, the reactor 100 is designed to process gasification feedstock, and the process fluid is provided in gaseous form. In an alternative embodiment, processing of essentially liquid feedstock material is not excluded.

[0055] Therefore, the reactor 100 is adapted for use in the heat treatment of hydrocarbon-containing feedstock. The heat treatment preferably involves the conversion of the feedstock to a desired product(s), thereby establishing conditions for at least one chemical reaction to occur in the process fluid. Alternatively, the process conditions within the reactor 100 may be adjusted so that conditions for chemical change (reaction) are not established during the heat treatment, thereby providing the reactor with a (pre)heater function.

[0056] In embodiments, the apparatus 100 is adapted for thermal and / or thermochemical hydrocarbon decomposition reactions, such as pyrolysis reactions, which collectively decompose hydrocarbon-containing feedstocks, optionally with the help of a diluent. Thus, the reactor 100 can be adapted for pyrolysis reactions with or without a diluent. Furthermore, the presence of a diluent is preferable as it improves the product yield.

[0057] Reactor 100 may be configured to receive feedstock diluted with at least one diluent, preferably a diluent gas such as (water) vapor. Steam is preferred as a diluent because, in the steam decomposition process, it lowers the hydrocarbon partial pressure to suppress or reduce the formation of coke deposits due to the gasification reaction(s). In some cases, the diluent is an inert gaseous medium such as hydrogen (H2), nitrogen (N2), or argon, which has substantially zero reactivity with the reactants and reaction products. The use of any other suitable diluent is not ruled out. In some cases, dilution is used to lower the partial pressure and increase the efficiency of the decomposition reaction to favor the production of the desired olefins (e.g., ethylene and propylene). In some other examples, reactor 100 may operate without a diluent.

[0058] In some configurations, the apparatus 100 is a steam decomposition reactor.

[0059] The reactor 100 comprises a rotor system (hereinafter referred to as the rotor) comprising a shaft 1 positioned along the horizontal (longitudinal) axis X-X' and a rotor unit mounted on the shaft 1. The reactor 100 further comprises at least one drive engine unit 1C (see Figures 8A-8C). The reactor 100 may utilize various drive engines such as electric motors, or may be directly driven by a gas turbine or steam turbine. A suitable coupling 1A is positioned between the drive shaft 1B and the rotor shaft 1 (see Figures 8A-8C). Depending on the configuration, flexible and rigid (non-flexible) shaft couplings 1A may be used. The rotor shaft 1 is supported by related bearing components, which will be further described below.

[0060] The rotor unit comprises a plurality of rotor blades 3 (also called actuarial blades) arranged around a disk 3a mounted on a rotor shaft 1. Together, the plurality of rotor blades arranged on the disk form a rotor blade assembly or rotor blade cascade (rotor cascade 3). The rotor blades 3 may consist of an axial flow blade profile, the term “axial flow” generally indicating that the process fluid flows into the rotor blade cascade from a direction essentially perpendicular to the rotor's rotation direction. Each rotor blade has a concave curved side (concave side) and a convex curved side (convex side). In a rotor cascade, the actuarial blades are mounted on the rotor disk with the concave side of each blade oriented in the direction of rotor rotation, as indicated by the arrow shape in Figure 1. In each actuarial blade (the top profile as seen in Figure 1), the direction from convex side to concave side is the direction of rotor rotation. As an example, the rotor blades may consist of a supersonic turbine blade profile.

[0061] The term "cascade" (crown of blades / vanes) refers to an assembly of (working) blades or (stationary) vanes arranged around the rotor disk or on a ring-shaped support or casing.

[0062] The reactor 100 further comprises stationary components. The stationary components are represented by a plurality of stationary (stator) vanes 2, 4 arranged in essentially annular assemblies or cascades (stator cascades 2, 4) on both sides of the rotor disc with blades. Thus, the first stator cascade 2 is located upstream of the rotor blade cascade 3, and the second stator cascade 4 is located downstream of the rotor blade cascade.

[0063] The terms “upstream” and “downstream” as used herein refer to the spatial and / or functional arrangement of a structural part or component (in this specification, a rotor disk with associated blade cascades) relative to a given part or component (in this specification, a rotor disk with associated blade cascades) in the direction of fluid flow throughout the reactor, essentially along the axis X-X', as shown in Figures 6A, 8A–8C and 9.

[0064] The stationary vane cascades are positioned adjacent to the rotor blades to form stator-rotor-stator arrays (SRSAs) 2, 3, and 4. When the reactor operates under design conditions, the distances between rotor and stator components within the SRSAs can be essentially the same.

[0065] The cascade located upstream of the rotor disc comprises a plurality of nozzle guide vanes (NGVs), also called nozzle vanes. These vanes form an annular nozzle guide vane cascade 2. The cascade located downstream of the rotor disc comprises a plurality of diffuser vanes, also called outlet guide vanes, which form an annular diffuser cascade (diffuser).

[0066] The first and second stationary vanes 2 and 4 have a curved profile which is preferably adjusted to match the supersonic flow velocity through the associated cascade. In reactor 100, the stationary vanes are installed such that the convex side of each vane is oriented in the direction of rotor rotation. Thus, in each stationary vane (the apex profile as seen in Figure 1), the direction from the concave side to the convex side is the direction of rotor rotation.

[0067] The reactor 100 further comprises a casing 6, in which an internal passage is formed in the form of a duct having at least one inlet 8 and at least one outlet 9. For the purposes of the present invention, the casing 6 is considered a stationary part. In this context, the term “stationary” is used in the sense of “non-rotating” and does not exclude the possibility of (axial) displacement, as further described below.

[0068] Figure 6A shows a reactor configuration having two inlets 8A, Figure 8B and two outlets 9A, Figure 9B, but other configurations are possible if necessary. For example, a reactor may include one inlet and one outlet, one inlet with two outlets, or two inlets with one outlet. Reactors with more inlets and / or outlets may be implemented. The inlets(single or more) and outlets(single or more) comprise associated openings / ports within the casing 6 and pipes, sleeves, or manifolds associated with each said port.

[0069] The casing 6 is configured to substantially completely surround the rotor disk, which has working blades assembled on it and stationary vane cascades 2, 4 adjacent to the rotor blades, forming a stator-rotor-stator array 2, 3, 4 as a whole. The casing 6 has an essentially toroidal ("donut-shaped") form in three dimensions, so that the rotor system (1, 3A, 3) with the associated bearing assemblies can be considered to fill an aperture defining an opening in the toroidal central portion. The toroidal structure is further referred to as the gas casing. In its meridional section, the gas casing 6 is essentially ring-shaped.

[0070] The reactor further comprises a flow straightener (flow guide) 5 located inside the gas casing 6. The flow straightener 5 may be configured as an internal stationary ring-shaped structure and serves to form an essentially annular duct inside the casing 6. The device 5 is fixed inside the gas casing 6 by appropriate fasteners (not shown). In some embodiments, the flow straightener 5 is an annular and essentially hollow structure, such as a hoop.

[0071] The internal volume of the reactor is defined as the space formed between the gas casing 6 (outer "donut") and the internal flow straightener 5 (inner "donut").

[0072] Therefore, a substantially annular passage / duct is formed between the inner surface of the gas casing 6 and the outer surface of the rectifier 5. Thus, this duct has a ring-shaped meridional cross-section. The rectifier 5, configured as an internal hoop, is adjacent to the tips of the rotor blades (a gap is formed between them to allow the rotor to rotate unimpeded) and the periphery of the stator vanes. In some embodiments, the stationary vane cascades 2, 4 may be mounted on bearing blocks that constitute the rotor bearing system, which will be described further below.

[0073] In some other examples, the stator cascade may be assembled on the rectifier 5 adjacent to the rotor blades 3. Thus, the stator vanes may be attached to and / or connected to the rectifier by auxiliary devices such as rings, brackets, etc. (not shown). The features described above represent the closest level of art and are detailed in publications by Bushuev (US Patent No. 9,494,038 (B2)) and Seppala et al. (US Patent No. 9,234,140), as mentioned above.

[0074] In the gas casing 6, cascades 2, 3, and 4 are adjacent to each other such that a vaneless space 7 is formed between the outlet from the stator-rotor-stator array (i.e., the outlet from the diffuser cascade 4) and the inlet to the array (i.e., the inlet to the nozzle guide cascade 2). The vaneless space is formed between the inner surface of the gas casing 6 and the outer surface of the rectifier 5. Most of the chemical reactions (one or more) that cause the conversion of the feed material(s) into the target product occur in the vaneless space.

[0075] By arranging dividing partitions (not shown) within the aforementioned annular passage / duct, a number of working cavities are formed inside the reactor. The dividing partitions are arranged symmetrically with respect to the rotor's axis of rotation. In this way, reactor configurations including, for example, two or four working cavities can be realized. Preferably, one or more inlet ports are located after each of the dividing partitions (in the direction of rotor rotation), and one or more outlet ports are located before each of the dividing partitions. In some examples, the annular duct may be implemented without division.

[0076] In the above-described configuration, the process fluid flow is configured to propagate through a duct forming the interior of the reactor following a helical trajectory. Cascades 2, 3, and 4 forming the stator-rotor-stator array direct the process fluid to repeatedly pass through the cascades and vaneless spaces 7, thereby forming a helical flow path within an essentially annular duct between at least one inlet and at least one outlet.

[0077] During operation, the (stationary) nozzle guide vanes 2 are configured to direct the process fluid flow into the rotor cascade. When provided as a stationary structure, the stator does not add energy to the process fluid. However, with respect to the profile, dimensions, and arrangement of the nozzle guide vanes around the rotor shaft 1, the nozzle guide vanes are configured to direct the process fluid flow into the rotor cascade in a predetermined direction in order to control, and in some cases maximize, the rotor's inherent work input capability.

[0078] The process fluid flow further flows into multiple rotor blades 3, which are configured to receive fluid flow from stationary vanes 2 as the rotor rotates, thereby adding mechanical energy to the process fluid by increasing the velocity of the fluid flow stream. The increase in flow velocity results in a corresponding increase in the kinetic energy of the fluid. The velocity of the flow stream passing through the stator-rotor-stator array is essentially supersonic.

[0079] The stationary vane-equipped diffuser 4 reduces the flow velocity and kinetic energy of the process fluid, causing the fluid to flow into the vaneless space 7 at subsonic speeds.

[0080] During its residence time in reactor 100, the process fluid passes through cascades 2, 3, and 4 several times. Each time it passes through rotor blade cascade 2, the process flow stream is accelerated, and as a result, it receives kinetic energy that would otherwise be dissipated into the internal energy of the reaction (process) fluid(s) as it propagates through diffuser 4 and vaneless space 7, supplying the thermal energy necessary 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 the fluid temperature. Therefore, high molecular weight compounds generated in the process fluid are effectively reduced in size.

[0081] Therefore, a process stage configured to mediate a complete energy conversion cycle is established when the process fluid flow stream propagates through the stationary nozzle guide vane cascade 2, rotor blade cascade 3, and stationary diffuser vane cascade 4 and reaches the vaneless space 7. During the energy conversion cycle, the mechanical energy of the fluid is converted into kinetic energy, which is further converted into the internal energy of the fluid, after which the fluid temperature rises and chemical reactions occur within the fluid.

[0082] During the residence time in reactor 100, the process fluid passes through cascade and vaneless spaces along a helical path, resulting in the establishment of several process stages (typically 5–10) during one process cycle. A process cycle is defined by the period during which flow particles are transferred with the process flow from inlet 8 to outlet 9 from the reactor, with the conversion of the feedstock compounds to the target product. Pyrolysis processes, including (steam) decomposition processes, require high temperatures and are highly endothermic; therefore, the reaction takes place at high temperatures (750–1000°C, typically 820–950°C), and residence times in the reaction zone are on a fraction of a second scale, such as approximately 0.5–0.1 seconds to 0.03–0.01 seconds (30–10 milliseconds). For completeness, it should be noted that the feedstock-containing process fluid flowing into the reactor is preheated to approximately 500–600°C.

[0083] Residence time affects the ratio of primary to secondary products at a given temperature. Therefore, under short residence times, primary reactions that lead to the formation of the target product (e.g., light olefins obtained by steam decomposition) are dominant, while longer residence times lead to an increase in secondary reactions, resulting in coke formation.

[0084] Overall, the reactor 100 is configured with respect to its geometric shape and stator and rotor-related parameters to establish conditions for at least one chemical reaction to occur within the process fluid.

[0085] The feedstock(s) contained in the process fluid flowing into the reactor, as they propagate through the reactor along the helical path as described above, are transformed to form the target product that exits the reactor with the fluid outflow. Throughout the process cycle, process conditions may require adjustments to facilitate the primary reaction that leads to the formation of the target product, while avoiding, or at least minimizing, the secondary reaction that typically results in coke formation.

[0086] The present invention is based on the observation that by adjusting the position of the rotor blade cascade 3 relative to the stationary vane cascades 2 and 4 in the stator-rotor-stator arrangement in the axial direction of the rotor shaft (i.e., the longitudinal direction of the rotor shaft 1 along axis X-X'), flow losses, in particular, flow leakage that occurs in the circumferential direction when the rotor rotates, can be adjusted with high efficiency.

[0087] Therefore, the concept of the present invention is based on adjusting the distance between the rotor blade cascade 3 and the stationary vane cascades 2, 4 along the longitudinal direction of the axis (X-X') defined by the rotor shaft. In some embodiments, the position of the rotor blade cascade relative to the stationary vane cascade can be adjusted by making the rotor axially displaceable (see Figures 8A, 8B, and 9).

[0088] In some alternative configurations, the position of the rotor blade cascade relative to the stationary vane cascade can be adjusted by the axial displacement of one or more stationary components. In some embodiments, the displaceable stationary component is the reactor casing 6 (see Figure 8C).

[0089] In rotary mechanical reactors, as described by Bushuev and Seppala et al. in the relevant patent publications, in most cases, a change in any one of the following: feedstock composition, feedstock consumption rate, or equipment-related and / or process-related parameters (e.g., rotor rotation speed, temperature, pressure, etc.) causes fluctuations in the fluid flow propagating through the reactor and the formation of leaks along the circumferential direction. In particular, leaks form in the direction from the inlet to the outlet, or from the end of one reaction zone to the beginning of an adjacent reaction zone. For example, increasing the process temperature (while the chemical composition of the feedstock-containing process fluid and its mass flow rate are essentially constant) is typically associated with the need to increase the rotor rotation speed. However, this causes flow leaks returning from the end of one reaction zone to the beginning of an adjacent reaction zone (see also Figure 3B), which then causes coke formation and can dramatically reduce the yield of the desired product.

[0090] Referring again to Figure 1, the arrangement of stator vanes 2, 4 relative to rotor blades 3 in reactor 100 operating under design conditions is shown. The design operating mode involves rotating the rotor at a design rotational speed U (also called circumferential speed or tangential speed). The direction of rotation of the rotor about the rotor axis is indicated by an arrow shape. For completeness, speed is defined as velocity relative to direction, otherwise the terms “speed” and “velocity” are used almost interchangeably.

[0091] Figure 1 shows the velocity triangle (V1, W1, α1, β1) of the fluid flow exiting the nozzle guide cascade 2 and flowing into the rotor cascade 3, and the velocity triangle (V2, W2, α2, β2) of the fluid flow exiting the rotor cascade and flowing into the diffuser cascade 4, 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) flows into the rotor blade, α2 (alpha 2) is the angle at which the absolute fluid flow (V2) flows into the stationary diffuser vane, β1 (beta 1) is the angle at which the relative fluid flow (W1) flows into the rotor blade, and β2 (beta 2) is the angle at which the relative fluid flow (W2) exits the rotor blade and flows into the stationary diffuser vane.

[0092] The inlet to a blade / vane cascade is generally defined by the leading edge of the associated blade / vane, and the outlet from the cascade is defined by the trailing edge of the blade / vane. The inlet and outlet are defined in the direction of the fluid flow.

[0093] Figures 2-5 are schematic diagrams of the stator-rotor-stator arrangement in reactor 100 operating under at least partially non-designed conditions. Velocities W1 and V2 are indicated by dashed arrows.

[0094] A reactor operating under design conditions (so-called design model) is defined as a reactor having a geometric shape designed and optimized to actually realize given input-related conditions, the inputs may relate to the state of the process fluid (its pressure, temperature, mass flow rate), the system (rotor speed, external temperature control, etc.), and / or the feedstock (a given load factor, chemical composition, etc.).

[0095] Out-of-design conditions are those in which the actual inputs used differ from the inputs for which the system was designed to operate. Out-of-design operation can be characterized by operating the system under fluctuating loads and / or with different feedstocks, by operating at temperatures, pressures, and / or mass flow rates different from the design point parameters.

[0096] Figure 2A shows the velocity triangle under operating conditions with a rotor rotation speed (U') slower than the rotor rotation speed (U) in the design mode, and Figure 3A shows the velocity triangle under operating conditions with a rotor rotation speed (U') faster than the rotor rotation speed (U) in the design mode.

[0097] Figure 4A shows the velocity triangle under operating conditions with the rotor rotation speed (U) in the design mode, but with increasing flow rate (here, mass flow rate with increased consumption of feed material flowing through the reactor). In such cases, the absolute velocity (V1') of the fluid flow leaving the nozzle guide cascade and flowing into the rotor cascade is faster than the absolute velocity (V1) of the fluid flow in the design mode.

[0098] Therefore, Figure 5A shows the velocity triangle under operating conditions with the rotor rotation speed (U) in the design mode, but with reduced flow rate (here, a mass flow rate with less consumption of feed material flowing through the reactor). In such a case, the absolute velocity (V1') of the fluid flow leaving the nozzle guide cascade and flowing into the rotor cascade is slower than the absolute velocity (V1) of the fluid flow in the design mode.

[0099] Therefore, Figures 2 to 5 show the velocity triangles obtained for the fluid flow (V1', W1', α1', β1') leaving the nozzle guide cascade and flowing into the rotor cascade, and the velocity triangles obtained for the fluid flow (V2', W2', α2', β2') leaving the rotor cascade and flowing into the diffuser cascade, in reactor 100 operating under non-design conditions different from the design conditions, where V' is the absolute velocity of the fluid flow and W' is the velocity of the fluid flow These are relative velocities, where α1' (alpha 1') is the angle at which the absolute fluid flow (V1') flows into the rotor blades, α2' (alpha 2') is the angle at which the absolute fluid flow (V2') leaves the rotor blades and flows into the stationary diffuser vanes, β1' (beta 1') is the angle at which the relative fluid flow (W1') flows into the rotor blades, and β2' (beta 2') is the angle at which the relative fluid flow (W2') leaves the rotor blades and flows into the stationary diffuser vanes.

[0100] Table 1 shows the fluid flow-related parameters for operating reactor 100 in design mode (U, V, W, α, β) and out-of-design mode (U', V', W', α', β'). [Table 1]

[0101] Based on the velocity triangle (Figures 2-5A), process fluid flow propagation paths (streamlines) are generated through the rotor blades in the reactor inlet region (inlet 8) and the reactor outlet region (outlet 9).

[0102] Figures 2–5B and 5C illustrate the effect of rotor axial displacement on controlling flow leakage in a reactor operating under non-design conditions. Similar measures apply when the distance between the rotor cascade and the stationary cascade in a stator-rotor-stator array is altered by the axial displacement of the casing.

[0103] Figure 2B shows the flow propagation paths at the design rotational speed (U: the relevant streamlines are shown as dashed lines) and the off-design rotational speed (U’), where the off-design rotational speed is slower than the design rotational speed (the relevant streamlines are shown as U’ < U). From Figure 2B, at the reduced rotational speed U’, it can be observed that a part of the flow stream directly propagates from the reactor inlet 8 to the outlet 9 from the reactor.

[0104] As can be seen from Figure 2B, reducing the rotational speed of the rotor causes leakage in the direction from the inlet to the outlet, and a part of the process stream does not flow into the reaction zone. In the pyrolysis reaction, this naturally leads to a decrease in the yield of the primary (target) product. The rotational speed of the rotor typically slows down when the temperature inside the reactor decreases. Other process parameters such as the chemical composition of the feedstock-containing process fluid and the mass flow rate of the process fluid through the reactor are essentially kept constant.

[0105] Figure 2C shows the situation where the rotor cascade 3 is shifted by shifting the rotor a predetermined distance ΔX (delta X), which is the displacement distance, in the direction of the nozzle guide cascade 2. By displacing the rotor, the relevant cascade 3 is displaced by a distance ΔX from its original position occupied by the cascade in the design mode. The displacement of the rotor occurs axially along the axis X-X’ (see Figures 6A, 8A - 8C, 9). The magnitude of the displacement defined by the value ΔX is selected such that when the rotor is shifted by that value, essentially all the flow streams proceed from the reactor inlet 8 towards the start of the reaction zone (rotational speed U’ < U).

[0106] Referring to Figures 2 - 5 and 7, the reaction zone is defined as the region within the duct formed between the gas casing 6 and the rectifying device 5, where the primary chemical reaction(s) that result in the formation of the target product occur during the process cycle defined above. Note that for clarity, most of the chemical reactions occur within the region / volume occupied by the vaneless space.

[0107] Figure 3B shows the flow propagation paths at the design rotational speed (U: associated streamlines are shown as dashed lines) and the out-of-design rotational speed (U'), where the out-of-design rotational speed is faster than the design rotational speed (associated streamlines are shown as U'>U). From Figure 3B, it can be observed that at the increased rotational speed U', a portion of the flow stream propagates back from the end of the reaction zone to the beginning of the reaction zone.

[0108] As can be seen from Figure 3B, with respect to the rotodynamic apparatus constituting this level of technology, as discussed above, increasing the rotor speed causes leakage in the direction from the end of the reaction zone back to the beginning of the adjacent reaction zone, and the primary product, once formed, returns to the beginning of the reaction zone without leaving the reactor. This leads to the formation of secondary reaction products, such as coke, and consequently the yield of the target product decreases accordingly. The rotor speed is typically set to a larger value as the temperature inside the reactor rises. As in the previous example, other process parameters such as the chemical composition of the feedstock-containing process fluid and the mass flow rate of the process fluid through the reactor are kept essentially constant.

[0109] Figure 3C shows a situation where the rotor is axially displaced by a predetermined distance ΔX away from the nozzle guide cascade 2. The magnitude of this displacement is selected so that essentially all flow streams from the end of the reaction zone proceed toward the reactor outlet 9 (at rotational speed U'>U).

[0110] Figure 4B shows the flow propagation paths at the design mass flow rate (flow entering the rotor at absolute velocity V1, relevant streamlines are shown as dashed lines) and the out-of-design mass flow rate V1', where the mass flow rate through the reactor increases (see streamlines V1'>V1). In both cases, the rotor rotation speed (U) is set in the design mode. From Figure 4B, it can be observed that at the increased mass flow rate (V1'), a portion of the flow stream propagates directly from the reactor inlet 8 to the reactor outlet 9.

[0111] Figure 4C shows a situation where the rotor is axially displaced by a predetermined distance ΔX in the direction of the nozzle guide cascade 2. The magnitude of this displacement is essentially selected such that all flow streams proceed from the reactor inlet 8 to the start of the reaction zone (with mass flow rate V1’ > V1).

[0112] Figure 5B shows the flow propagation paths at the design mass flow rate (the relevant streamlines are shown by dashed lines where the flow enters the rotor at absolute velocity V1) and the off-design mass flow rate V1’, and the mass flow rate through the reactor decreases (see streamline V1’ < V1). In both cases, the rotational speed (U) of the rotor is set in the design mode. From Figure 5B, it can be observed that at the reduced mass flow rate V1’, a part of the flow stream propagates such that it returns from the end of the reaction zone to the start of the reaction zone.

[0113] Figure 5C shows a situation where the rotor is axially displaced by a predetermined distance ΔX in the direction opposite to the nozzle guide cascade 2. The magnitude of this displacement is essentially selected such that all flow streams from the end of the reaction zone proceed towards the reactor outlet 9 (with mass flow rate V1’ < V1).

[0114] As shown in Figures 2 - 5C, the rotor is configured to be axially displaceable. The displacement is achieved for the entire rotor by a bearing mechanism that will be described in more detail below. The displacement of the rotor shifts the associated rotor cascade 3 by a preselected distance ΔX relative to the stationary reactor components.

[0115] The displacement distance of the exemplary device 100 can be 5 - 15 mm (see also Example 1). Further, it is clear that the magnitude of the axial displacement distance can vary depending on the size, type, design, and / or purpose of the reactor.

[0116] An additional or alternative solution may involve shifting the rotor disk 3A along the rotor shaft 1 (not shown).

[0117] In the configuration described with reference to Figures 2 to 5, the rotor 3 is configured to be axially displaceable in the direction of the stationary vane cascade located upstream of the rotor blade cascade (i.e., the nozzle guide vane cascade). This is demonstrated by positioning a displaceable bearing in the vicinity of the rotor drive unit. In the reactor described herein, the disk having the associated blade cascade is positioned between the annular vane cascades, and therefore, displacement of the rotor cascade toward either of the stationary cascades alters the original position of the rotor blades relative to both stator cascades. For clarity, the stationary vanes are not axially displaceable.

[0118] Therefore, in some embodiments, the present invention involves adjusting the position of the rotor blade cascade 3 relative to the stationary vane cascades 2 and 4 in a stator-rotor-stator array by providing a rotor that is axially displaceable by a predetermined distance (ΔX) in the longitudinal direction of the rotor shaft (X-X') relative to the stationary components of the reactor (i.e., stationary vane cascades 2 and 4 and the casing 6).

[0119] In some configurations, the rotor is displaced longitudinally by a predetermined distance (ΔX) toward a stationary vane cascade 2 located upstream of the rotor blade cascade 3 when the rotor rotational speed (U) decreases and / or when the flow rate of process fluid through the reactor increases. In practice, the modified flow rate refers to the modified mass flow rate caused by the increase in the consumption of feedstock material.

[0120] In some other configurations, the rotor is displaced longitudinally by a predetermined distance (ΔX) away from a stationary vane cascade 2 located upstream of the rotor blade cascade 3 when the rotor rotation speed increases and / or when the flow rate of process fluid through the reactor decreases. In practice, the modified flow rate refers to the modified mass flow rate caused by the decrease in the consumption of feedstock material.

[0121] In some embodiments, the distance between the rotor blade cascade 3 and the stationary vane cascades 2, 4 along the rotor shaft is adjusted by making one or more stationary components of the reactor displaceable along the rotor shaft. The stationary component(s) are displaced by a predetermined distance (ΔX) along the rotor shaft (in the X-X' direction). In such cases, the rotor remains shifted. Alternatively, the axial movement of the stationary component may be accompanied by the axial movement of the rotor.

[0122] For example, the axial displacement of the casing 6 may be accompanied by the axial displacement of at least one stationary vane cascade (e.g., nozzle guide vane cascade 2) as these elements are constructed in relation to one another.

[0123] For example, by shifting the rotor and / or stationary components, the position of the rotor blade cascade can be changed in the manner described above, allowing for highly precise control of flow leakage. The amount and / or direction (from inlet to outlet, from the end of one reaction zone to the beginning of an adjacent reaction zone) can be efficiently controlled.

[0124] Changes in (mass) flow rate and associated feedstock consumption can be further compensated for by modifying the feedstock-to-diluent ratio (where the diluent is, for example, (water) vapor) so that the total flow rate of the feedstock-containing process fluid (i.e., feedstock / diluent mixture) through the reactor remains constant.

[0125] For example, as described above, adjustment of the position of the rotor blade cascade relative to the stationary vanes due to the axial displacement of the rotor may be performed in reactor 100 set to operating mode or non-operating mode. In this context, "operating mode" refers to the state of apparatus 100 resulting from the use or application of apparatus 100, and optionally means setting the rotor to rotate. Such use may occur, for example, during normal operation (meaning the execution of one or more chemical reactions in the reaction) or system testing. Non-operating mode, on the other hand, generally means that apparatus 100 is stopped or shut down.

[0126] Performing rotor displacement in a reactor set to non-operating mode is typically done when the reactor must be adapted for use with feedstock that differs from that previously used (e.g., different in terms of origin and / or various chemical compositions), because such adaptations may require other adjustments within the system.

[0127] Rotor displacement can be performed by setting the reactor to an operating mode. In such cases, axial shifting can be performed manually or automatically, allowing for automatic adjustment of axial rotor movement, controlled by a local or centralized control system (not shown). In some cases, axial displacement can be performed without stopping the rotor's rotation. In such cases, reducing the rotor's rotational speed may be advantageous.

[0128] Similar considerations apply to the axial displacement of stationary components (one or more).

[0129] Any combination of the above-described methods can be used to adjust for flow losses resulting from circumferential leakage.

[0130] Referring further to Figures 6A and 6B, Figure 6A shows a reactor 100 according to one embodiment, and Figure 6B shows a cross-sectional view along lines AA and BB designed in Figure 6A. The cross-sectional region along line AA is located at the inlet to the nozzle guide vane cascade 2, and the cross-sectional region along line BB is located at the outlet from the diffuser cascade 4. Overall, cross-sectionals AA and BB show the events occurring at the inlet to the stator-rotor-stator array and the outlet from the stator-rotor-stator array.

[0131] The locations where process streamlines enter and exit the reactor are shown in the images of cross-sections AA and BB (Figure 6B). Furthermore, process streamlines passing through the stator-rotor-stator arrays 2, 3, and 4, which generally follow a helical path, are shown as separately numbered sector regions or sectors (see Roman numerals i-vii). A flowchart illustrating the streamline pathways through the reactor is shown on the right. Figure 6B shows streamlines traveling between the first inlet 8A and the first outlet 9A (streamlines traveling between the second inlet 8B and the second outlet 9B are not shown).

[0132] During operation, the process fluid flow containing the feedstock enters the reactor through the inlet opening 8 (here 8A) and reaches the first stationary vane cascade 2 (nozzle guide vane cascade). In section AA, the inlet region within the first stationary vane cascade 2 is shaded (Figure 6B). Several stationary vanes located in the inlet region are connected to the associated inlet openings by dividing partitions (one or more), thereby forming an operating cavity between the inlet and outlet.

[0133] The fluid flow stream propagates through the stator-rotor-stator array 2, 3, 4, which in fact means that the flow stream propagates sequentially through the (stationary) nozzle guide vanes 2, the (rotating) rotor blades 3, and the (fixed) diffuser vanes 4, after which the flow stream exits the cascade (singular or plural) at sector (i) of the diffuser cascade (section BB) and flows "upward" through the vaneless space 7. The flow enters the vaneless space after exiting the second stationary vane cascade 4 (diffuser vane cascade).

[0134] Each time the process fluid propagates through the stator-rotor-stator cascade, the temperature of the process stream rises, which in turn promotes one or more chemical reactions in the vaneless spaces located downstream of the cascade in the direction of fluid flow.

[0135] After passing through the vaneless space 7, the flow stream reaches sector (i) (section AA) of the nozzle guide vane cascade 2, and the process described above is repeated. That is, the fluid flow stream proceeds through cascades 2, 3, and 4, exits sector (ii) (section BB) of the diffuser cascade 4, and continues flowing through the vaneless space 7 towards sector (ii) (section AA) of the nozzle guide vane cascade 2, following a generally helical path. In the configuration shown in Figure 6B, the flow stream propagates through the cascades eight times (thus forming eight stages). After the final propagation (in this case, the eighth) through the stator-rotor-stator cascade, the flow stream exits the cascade and proceeds from the reactor to outlet 9 (in this case, 9A).

[0136] In section BB, the exit region within the second stationary vane cascade 4 is shaded. Several stationary vanes located in the exit region are connected to the associated exit opening by a dividing partition wall(s) (one or more).

[0137] Refer to Figures 8A to 8C, which schematically show various configurations for axial displacement of the rotor (Figures 8A and 8B) and stationary components (Figure 8C).

[0138] In all basic embodiments, the reactor 100 comprises a (gas) casing 6 surrounding a rotor cascade 3 and annular stationary vane cascades 2 and 4 located on either side of the rotor. A flow straightener 5 in the form of a hollow hoop is installed inside the casing 6, thereby forming an annular duct between the inner surface of the casing 6 and the outer surface of the flow straightener 5. The portion of the duct not occupied by vanes / blades forms a vaneless space 7.

[0139] The reactor, embodied as 100A (Figure 8A), further comprises at least one thrust bearing element 23 (also called a thrust sliding bearing) positioned on the rotor shaft 1. The thrust bearing(s) support axial loads acting parallel to the axis of the shaft. The thrust bearing element 23 may be configured, for example, as a hydrodynamic thrust bearing in which a thrust disc 23A is fitted between corresponding pads or races. Any other suitable configuration may be utilized.

[0140] The thrust bearing element 23 is configured to be displaceable along the rotor shaft 1 relative to the stationary components of the reactor (e.g., the casing 6). Thus, in the configuration of Figure 8A, the rotor is made axially displaceable via the axial displacement of the thrust bearing element 23. In such a configuration, the shaft coupling 1A positioned between the rotor shaft 1 and the drive shaft 1B is advantageously configured as a flexible coupling capable of axially displacing either (or both) of the drive shaft and the rotor shaft.

[0141] Figure 8B shows a configuration 100B in which the rotor is made axially displaceable by the axial displacement of the drive shaft 1B (the drive shaft 1B is connected to the rotor shaft 1 via a coupling 1A). The coupling 1A may be provided in the form of a rigid (preferred) or flexible coupling. The reactor 100B can be implemented without thrust bearings (one or more).

[0142] In some specific configurations, the reactor 100B is implemented without thrust bearings, the drive shaft 1B is configured to be axially displaceable, and the coupling 1A positioned between the drive shaft 1B and the rotor shaft 1 is (axially) inflexible, i.e., does not allow mutual displacement between the drive shaft and the rotor shaft.

[0143] Configurations 100A and 100B (Figures 8A and 8B) are characterized by fixed, stationary components. In particular, the reactor casing is configured to be immovable (impossible to displace) relative to the reactor drive unit 1C. In both configurations, axial reciprocating motion of the rotor is possible.

[0144] Configurations 100A and 100B may involve providing sliding radial bearings (journal bearings) (optionally within related blocks) longitudinally positioned on the rotor shaft 1 on both sides of the rotor disc 3A (see the description in Figure 9 for details).

[0145] Figure 8C shows a configuration (100C), in which the position of the rotor blade cascade 3 relative to the stationary vane cascades 2, 4 in the stator-rotor-stator arrangement is adjustable by axially displacing at least one stationary component, in particular the reactor casing 6, along the longitudinal direction of the rotor shaft. Displacement of either the casing 6 or any one of the stationary vane cascades 2, 4 can be performed via sliding radial bearings 22, 32 (see description in Figure 9).

[0146] Overall, the reactor 100 can be implemented without thrust bearings (one or more) 23 (e.g., form 100C).

[0147] In the device 100C, the drive shaft 1B is preferably fixed in the axial direction (impossible to displace). Furthermore, the coupling 1A is preferably configured in a rigid (inflexible) form in order to prevent the drive shaft 1B and rotor shaft 1 from being displaced in the axial direction.

[0148] In some specific configurations, the reactor 100C is implemented without thrust bearings, the drive shaft 1B is configured to be immovable in the axial direction, and the coupling 1A positioned between the drive shaft 1B and the rotor shaft 1 is also immovable, thereby preventing axial displacement between the drive shaft and the rotor shaft.

[0149] In this disclosure, the gas casing 6 is generally referred to as the reactor casing. Nevertheless, the apparatus structure 100 (100A, 100B, 100C) may be further enclosed within a separate external housing (not shown).

[0150] Referring to Figure 9, an exemplary mechanism for axial rotor displacement in reactor 100 is shown, the mechanism involving the displacement of a thrust bearing. Overall, the embodiments 100, 100A shown in Figure 9 are based on the configuration shown in Figure 8A, and thus repetition is avoided when describing the basic embodiments.

[0151] In the embodiment shown in Figure 9, the reactor comprises a bearing system comprising radial (sliding) bearing elements 22, 32 and at least one thrust bearing element 23. In some embodiments, the radial bearing elements are journal bearings longitudinally positioned on the rotor shaft 1 on both sides of the rotor disc 3A. The radial bearings support rotor loads acting perpendicular to the axis of the rotor shaft. Each radial bearing element 22, 32 is fitted into housings 22A, 32A (radial bearing housings) and supported by appropriate O-ring seals 39 (the other side is not shown).

[0152] At least one thrust bearing 23 is positioned on the rotor shaft adjacent to the radial bearing. Any suitable radial (journal) and thrust bearing configuration can be utilized.

[0153] Therefore, in some configurations, the bearing system is implemented using a pair of radial bearings 22, 32, where the radial bearing elements 22 and thrust bearing elements 23, positioned adjacent to each other on the rotor shaft on one side of the rotor disc, are housed within a housing 21 to form a first bearing block. The radial bearing element 32, positioned on the rotor shaft on the other side of the rotor disc, is housed within the housing 31 to form a second bearing block. These bearing blocks are installed on both sides of the gas casing 6.

[0154] The thrust bearing element is preferably mounted on the rotor shaft in the vicinity of the rotor drive unit (i.e., on the side of the rotor disc coupled to the drive engine).

[0155] The bearing block located at the front / inlet end of the reactor (i.e., the end where the nozzle guide vane cascade 2 is located) is called the first bearing block, and the bearing block located at the rear / outlet end of the reactor (i.e., the end where the diffuser vane cascade 4 is located) is called the second bearing block. Each of the first and second bearing blocks comprises bearings, and optionally bearing assemblies, fitted into corresponding housings 21, 31 (bearing block housings). The bearing assemblies described above are configured to absorb radial loads and, advantageously, axial (thrust) loads as well.

[0156] In the apparatus shown in Figure 9, the thrust bearing element 23 is housed in a separate housing 24 (thrust bearing housing), which at least partially surrounds the housing 21 of the associated bearing block. The (rotor shaft) end sealing 29 is installed inside the thrust bearing housing 24 under the thrust bearing housing cover 24A.

[0157] Additionally or alternatively, the thrust bearing may be housed within a second bearing block (not shown).

[0158] Lubricating oil is supplied to the bearing blocks from an oil system (not shown) through corresponding oil inlet channels 25, 35 in the block housings 21, 31. The oil is discharged from the bearings through oil outlet channels 26, 36. Separate oil channels (inlet and outlet) are located within the thrust bearing housing 24 to lubricate and cool the thrust bearing housing 24.

[0159] The bearing block may further include labyrinth seals 27, 37. To avoid contamination of process fluids and / or the generation of excessive heat during the process, liquid-free labyrinth seals, such as gas labyrinth seals, may be used. To provide the seal, an inert gas such as steam (water vapor) or nitrogen may be used. The inert gas is supplied into the labyrinth seal through channels 28, 38.

[0160] In some configurations, each of the stationary vane cascades 2, 4 and optionally the outer casing 6 are fixed onto the bearing block.

[0161] The enclosed (24) thrust bearing element 23 is configured to be axially displaceable by a predetermined distance ΔX in the longitudinal direction of the rotor shaft (along the axis X-X') within the associated bearing block. The thrust bearing 23 is displaceable relative to the housing 21 of the bearing block. Being displaceable relative to the bearing block housing also allows the thrust bearing element 23 to be displaceable relative to stationary components of the reactor (e.g., the casing 6).

[0162] As described above, the rotational motion of the rotor is supported by radial bearings 22 and 32 installed along the rotor shaft 1. On the other hand, the thrust bearing element 23 allows for axial displacement of the rotor.

[0163] Therefore, in the embodiment of Figure 9, the rotor is made axially displaceable relative to the stationary vane cascades 2, 4 and the gas casing 6 by adjusting the position of the (24) thrust bearing element 23 surrounding the rotor shaft in the longitudinal direction of the bearing block relative to the housing 21 of the bearing block. This allows the rotor to reciprocate in the axial direction.

[0164] The device 100 can be implemented according to the following example.

[0165] Example 1. The apparatus 100 comprises a gas casing 6 having two inlets 8A, 8B and two outlets 9A, 9B. The casing surrounds a rotor 3 and annular stationary vane cascades 2, 4 fixed to both sides of the rotor. A rectifier 5 in the form of a hollow hoop is installed within the casing, forming an annular duct, and the portion of the duct not occupied by vanes / blades forms a vaneless space 7. The rotor is configured to be displaceable along the longitudinal axis X-X'. The reactor 100 operates with parameters defined in Table 2. [Table 2]

[0166] In the apparatus 100 designed and implemented using the parameters in Table 2, the rotor must be axially displaced by a distance ΔX equal to 6.6 mm in the direction of the nozzle guide vane cascade in order to avoid or at least minimize circumferential flow leakage resulting from a 25% reduction in rotational speed U.

[0167] The effect of this displacement is shown in more detail in Figure 7, where Figure 7A shows the velocity triangle obtained in reactor 100 according to the design parameters (numerical values ​​are expressed in millimeters) listed in Table 2.

[0168] Figure 7B shows the velocity triangle under out-of-design operating conditions with a 25% reduction in rotational speed U' compared to the rotational speed U in the design mode. Velocities W1 and V2 are indicated by dashed arrows.

[0169] Figure 7C shows a situation where the rotor cascade 3 is displaced by a distance ΔX in the direction of the nozzle guide vane cascade 2. In this case, ΔX = 6.6 mm. With the selected magnitude of displacement, essentially all flow entering the reactor is forced to the beginning of the reaction zone.

[0170] Device 100, configured using the blade parameters listed in Table 2, is also shown in Figure 9. Note that the displacement distance ΔX is 8 mm. Where applicable, numerical values ​​in the figures (one or more) are expressed in millimeters.

[0171] In all the forms described above, the peripheral (rotational) speed of the rotor (U) can be set within the range of 150 to 400 m / s. This speed depends on how much energy needs to be supplied to the process flow for a given composition of the raw material.

[0172] The axial size of the rotor blades can be set within the range of 20 to 90 mm. The clearance between the nozzle guide vane cascade and the rotor blade cascade in the axial direction can be set within the range of 6 to 40 mm. Overall, the dimensions of the rotor blades and stationary vanes, as well as the clearance between them, are determined according to the size of the reactor 100 and its performance capabilities.

[0173] In a reactor having the specifications described above, the displacement distance ΔX may vary within a range of approximately 0.5 to 25 mm, and this range may be widened when the apparatus is enlarged.

[0174] A reactor configuration can be realized by connecting at least two reactors 100 in parallel or in series (not shown). The connection between the reactors may be mechanical and / or functional. A functional connection (e.g., with respect to chemical properties) can be realized when at least two individual physically integrated or disintegrated reactors 100 are coupled. If they are not physically integrated, the coupling between the at least two reactors 100 may be realized via some auxiliary equipment (not shown). In some embodiments, the configuration comprises at least two reactors that are at least functionally connected via their central shaft. Such embodiments may be further defined as at least two reactors 100 being mechanically connected in series (sequentially), although a functional connection (e.g., with respect to feedstock-based reactions) may be considered as being connected in parallel (in a series).

[0175] In some examples, the configuration may further include a preheating furnace (here, a furnace). Together, the furnace and at least one reactor 100 may form a cracker unit (not shown). Several parallel reactors 100 may be connected to a common furnace, or several reactors 100 may be connected to several furnaces.

[0176] In a further embodiment, the use of the apparatus 100 and / or related configurations is provided for the thermal or thermochemical conversion of hydrocarbon-containing feedstock.

[0177] In the selected form, the conversion is thermal or thermochemical decomposition of the hydrocarbon-containing feedstock, in particular fluid hydrocarbon-containing feedstock (i.e., fluid organic feedstock material mainly containing carbon and hydrogen).

[0178] Additionally or alternatively, reactor 100 may be configured to process oxygen-containing feedstock materials such as oxygen-containing hydrocarbon derivatives. In some forms, reactor 100 may be adapted to process cellulosic feedstocks. In some additional or alternative forms, reactors may be adapted to process (waste) animal fat-based and / or (waste) vegetable oil-based feedstocks. The pretreatment of the animal fat-based and vegetable oil-based feedstocks may include hydrodeoxygenation (removal of oxygen from oxygen-containing compounds), which results in the decomposition of (tri)glyceride structures, yielding mostly linear alkanes. In further additional or alternative forms, reactor 100 may be adapted to process by-products of the wood pulp industry such as tall oil or any derivative thereof. The definition of “tall oil” refers to the commonly known by-products of the kraft process, used primarily in the pulping of softwoods in wood pulp production.

[0179] In this process, the hydrocarbon-containing feed provided may include, but are not limited to, one of the following: intermediate heavy hydrocarbons such as naphtha and diesel fuel, and light hydrocarbons such as ethane, propane, and butane. Propane and heavier fractions may also be utilized.

[0180] In some cases, the hydrocarbon-containing feed is gasified, pre-treated biomass material. The biomass feed is pre-treated biomass derived from cellulose, or especially lignocellulose, supplied to the reactor in substantially gaseous form.

[0181] Hydrocarbon-containing feedstocks may further be provided as either pre-treated glyceride-based materials such as (waste or residual) vegetable oils and / or animal fats, or pre-treated plastic waste or residues. The pre-treatment of the (tri)glyceride-based feedstocks may include different processes such as pyrolysis or deoxygenation as described above. Various plastic wastes, including PVC materials, PE materials, PP materials, PS materials and mixtures thereof, may be further used as feedstocks for manufacturing new plastics and / or utilized in pyrolysis oil or gas recovery processes that can be refined into fuel oil(s) (diesel fuel equivalents).

[0182] Accordingly, in selected embodiments, the reactor 100 may be configured to perform at least one procedure selected from the group consisting of processing hydrocarbon feedstocks preferably containing medium and light hydrocarbon fractions, processing feedstocks containing gaseous carbohydrates, processing feedstocks containing gaseous glycerides and / or fatty acids, and processing gaseous cellulosic biomass materials. Thus, the reactor 100 can be configured to process, for example, oxygen-containing feedstocks derived from bio-based feedstocks. Possible application areas include, for example, the purification of biomass-based or biomass-derived materials for producing renewable fuels in processes such as the direct catalytic hydrogenation of vegetable oils or animal fats to corresponding alkanes or the catalytic dehydrogenation of gaseous hydrocarbons as one step in the Fischer-Tropsch process. Furthermore, the reactor may be configured for price stabilization (increase or purification of gaseous substances) of bio-based pyrolysis gases or synthesis gases.

[0183] When using feedstocks based on biomass, glyceride, and / or polymeric materials, reactor 100 can be further adapted to a catalytic process. This is achieved by several catalyst surfaces (not shown) formed by catalyst coatings (one or more) on reactor blades or inner walls in contact with the process fluid(s). In some cases, the reactor may comprise several catalyst modules defined by ceramic or metal substrates (one or more) or support carriers (one or more) having an active (catalytic) coating, which is optionally realized as a monolithic honeycomb structure.

[0184] In another embodiment, a method is provided for improving process efficiency and adjusting flow losses during processing of feedstock in a process fluid. The method is (a) A step of acquiring the device (100), -A rotor comprising multiple rotor blades arranged around a disk (3a) attached to a rotor shaft (1), forming a rotor blade cascade (3), - A plurality of stationary vanes arranged in an annular vane cascade (2, 4) adjacent to the rotor blade cascade so as to form a stator-rotor-stator arrangement (2, 3, 4), - A duct is formed having at least one inlet (8) and at least one outlet (9), and a casing (6) surrounds the rotor blade cascade (3) and the stationary vane cascade (2, 4) within the duct. The steps include obtaining an apparatus 100 equipped with, (b) A step of adjusting the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator array by a predetermined distance (ΔX) in the axial direction along the rotor shaft. It includes at least [this].

[0185] This method is particularly advantageous when operating the device 100 under non-design conditions.

[0186] In this method, the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator arrangement is adjusted by axially displacing the rotor in the longitudinal direction of the rotor shaft. Alternatively, a stationary component (e.g., casing) can be displaced. This allows for reciprocating motion of either the rotor or the stationary component in the longitudinal direction along the rotor shaft.

[0187] In some embodiments, adjusting the position of the rotor blade cascade relative to the stationary vane cascade in the stator-rotor-stator array involves adjusting at least the rotor rotation speed and / or the flow rate of the feedstock-containing process fluid. In some cases, adjusting the flow rate includes adjusting the mass flow rate, which indicates the total consumption of feedstock material.

[0188] In some configurations, the rotor is displaced longitudinally by a predetermined distance ΔX toward a stationary vane cascade 2 (nozzle guide vane cascade) located upstream of the rotor blade cascade 3 when the rotational speed of the rotor decreases and / or when the flow rate of process fluid through the reactor 100 increases.

[0189] In some other configurations, the rotor is displaced longitudinally by a predetermined distance ΔX away from a stationary vane cascade 2 located upstream of the rotor blade cascade 3 when the rotational speed of the rotor increases and / or when the flow rate of process fluid through the reactor 100 decreases.

[0190] In this method, the positions of the rotor and / or stationary components can be adjusted within the device, which is set to operating mode or non-operating mode.

[0191] In this method, the feedstock preferably includes hydrocarbons. In some cases, the feedstock includes at least one alkane feedstock (ethane, propane, butane), naphtha feedstock, diesel fuel, and / or essentially low molecular weight hydrocarbons, preferably unsaturated hydrocarbons, such as olefins (ethylene, propylene, butylene) and any other feedstock suitable for producing acetylene.

[0192] It will be apparent to those skilled in the art that, with advances in technology, the basic concepts of the present invention can be implemented in various ways. The present invention and its embodiments may generally be modified within the scope of the appended claims.

Claims

1. An apparatus (100) for processing a feed material in a process fluid, wherein the apparatus (100) is Rotor shaft (1) and A rotor comprising a plurality of rotor blades arranged around a disk (3a) attached to the rotor shaft (1), forming a rotor blade cascade (3), Multiple stationary vanes arranged in an essentially annular vane cascade (2, 4) adjacent to the rotor blade cascade so as to form a stator-rotor-stator arrangement (2, 3, 4), A casing (6) in which a duct having at least one inlet (8) and at least one outlet (9) is formed, the casing surrounds the rotor blade cascade (3) and the stationary vane cascade (2, 4) within the duct, A flow straightening device (5) is provided, wherein the flow straightening device (5) is positioned inside the casing (6) such that the duct is formed between the inner surface of the casing (6) and the outer surface of the flow straightening device (5), Equipped with, A vaneless space (7) is formed between the outlet from the stator-rotor-stator array (2, 3, 4) and the inlet to the stator-rotor-stator array (2, 3, 4), and the vaneless space (7) is defined by a portion of the duct between the casing (6) and the rectifier (5) that is not occupied by blades and vanes. The cascade within the stator-rotor-stator array (2, 3, 4) is configured to direct the process fluid so that it repeatedly passes through the cascade and the vaneless space (7) in a helical flow path as it propagates through the duct between the at least one inlet (8) and the at least one outlet (9), thereby establishing conditions for at least one chemical reaction to occur within the process fluid. The device (100) is such that the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement can be adjusted axially along the rotor shaft by a predetermined distance (ΔX).

2. The apparatus (100) according to claim 1, wherein the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement can be adjusted by axially displacing the rotor in the longitudinal direction of the rotor shaft.

3. The apparatus (100, 100A) according to claim 1 or 2, further comprising at least one thrust bearing element (23) disposed on the rotor shaft, wherein the rotor is axially displaceable by the axial displacement of the at least one thrust bearing element on the rotor shaft.

4. The apparatus (100, 100A) according to claim 3, wherein at least one thrust bearing element (23) is configured to be displaceable in the axial direction relative to the casing (6).

5. The apparatus (100, 100A) according to any one of claims 3 to 4, wherein the thrust bearing element (23) is housed in a separate housing (24) at least partially enclosed within the bearing block (21), and the enclosed thrust bearing element (23, 24) is configured to be axially displaceable in the longitudinal direction of the rotor shaft within the associated bearing block.

6. The apparatus (100, 100A) according to any one of claims 1 to 5, wherein the apparatus (100) further comprises a drive shaft (1B), and the coupling (1A) disposed between the rotor shaft (1) and the drive shaft (1B) is a flexible shaft coupling configured to allow the drive shaft and the rotor shaft to be displaced in the axial direction.

7. The apparatus (100, 100B) according to claim 6, wherein the drive shaft (1B) is connected to the rotor shaft (1) via the coupling (1A), and the rotor is made axially displaceable by the axial displacement of the drive shaft (1B).

8. The apparatus (100, 100C) according to any one of claims 6 to 7, wherein the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement can be adjusted by axially displacing the casing (6) in the longitudinal direction of the rotor shaft.

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

10. The apparatus according to any one of claims 7 to 9, wherein the coupling (1A) is a rigid shaft coupling configured to prevent axial displacement of the drive shaft and the rotor shaft.

11. The apparatus (100) according to any one of claims 1 to 10, wherein each of the stationary vane cascades (2, 4) is fixed on associated bearing blocks (21, 31) located on both sides of the casing (6).

12. Apparatus (100) according to any one of claims 1 to 11, wherein the adjustment of the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement is accompanied by adjustment of at least the rotational speed of the rotor and / or the flow rate of the feed material-containing process fluid.

13. The apparatus (100) according to any one of claims 1 to 12, wherein the duct has a ring-shaped meridional cross-section.

14. The apparatus according to any one of claims 1 to 13, wherein the rectifier (5) has an annular and essentially hollow structure.

15. The apparatus (100) according to any one of claims 1 to 14, wherein the stationary vane cascade is formed by a plurality of stationary nozzle guide vanes that form an annular nozzle guide vane cascade (2) on the upstream side of the rotor blade and a plurality of stationary diffuser vanes that form a diffuser vane cascade (4) on the downstream side of the rotor blade.

16. The apparatus (100) according to any one of claims 1 to 15, comprising several catalyst surfaces.

17. The apparatus (100) is an apparatus (100) according to any one of claims 1 to 16, used for heat treatment of hydrocarbon-containing feedstock.

18. The apparatus (100) is an apparatus (100) according to any one of claims 1 to 16, used to carry out a chemical reaction.

19. The apparatus (100) according to claim 17 or 18, wherein the apparatus (100) is used for thermal or thermochemical decomposition of a hydrocarbon-containing feedstock.

20. The apparatus (100) according to any one of claims 17 to 19, wherein the apparatus (100) is used to perform at least one procedure selected from the group consisting of processing a hydrocarbon feedstock containing medium and light hydrocarbon fractions, processing a feedstock material containing gaseous carbohydrates, processing a feedstock material containing gaseous glycerides and / or a feedstock material containing fatty acids, and processing a gaseous cellulosic biomass material.

21. A configuration comprising at least two devices according to any one of claims 1 to 20, functionally connected in parallel or in series.

22. A method for improving process efficiency and adjusting flow losses during processing of feedstock in a process fluid, wherein the method is a. A step of acquiring the device (100), wherein the device (100) is A rotor comprising a plurality of rotor blades arranged around a disk (3a) attached to a rotor shaft (1), forming a rotor blade cascade (3), Multiple stationary vanes are arranged in an annular vane cascade (2, 4) which is positioned adjacent to the rotor blade cascade so as to form a stator-rotor-stator arrangement (2, 3, 4), A duct is formed having at least one inlet (8) and at least one outlet (9), and a casing (6) surrounds the rotor blade cascade (3) and the stationary vane cascade (2, 4) within the duct, A flow straightening device (5) is provided, wherein the flow straightening device (5) is positioned inside the casing (6) such that the duct is formed between the inner surface of the casing (6) and the outer surface of the flow straightening device (5), A step comprising, b. The step of adjusting the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement by a predetermined distance (ΔX) along the rotor shaft in the axial direction, c. A step of forming a vaneless space (7) between the outlet from the stator-rotor-stator array (2, 3, 4) and the inlet to the stator-rotor-stator array (2, 3, 4), wherein the vaneless space (7) is defined by a portion of the duct between the casing (6) and the rectifier (5) that is not occupied by blades and vanes. Methods that include...

23. The method according to claim 22, wherein the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement is adjusted by axially displacing the rotor in the longitudinal direction of the rotor shaft.

24. The method according to claim 22, wherein the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement is adjusted by axially displacing the casing (6) in the longitudinal direction of the rotor shaft.

25. The method according to any one of claims 22 to 24, wherein the adjustment of the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement is accompanied by adjustment of at least the rotational speed of the rotor and / or the flow rate of the feed material-containing process fluid.

26. The method according to claim 22 or 23, wherein the rotor is displaced by a predetermined distance (ΔX) in the longitudinal direction toward a stationary vane cascade (2) located upstream of the rotor blade cascade (3) when the rotational speed of the rotor decreases and / or when the flow rate of process fluid through the apparatus (100) increases.

27. The method according to claim 22 or 23, wherein the rotor is displaced by a predetermined distance (ΔX) in the longitudinal direction away from the stationary vane cascade (2) located upstream of the rotor blade cascade (3) when the rotational speed of the rotor increases and / or when the flow rate of process fluid through the apparatus (100) decreases.

28. The method according to any one of claims 22 to 27, wherein the adjustment of the position of the rotor blade cascade (3) relative to the stationary vane cascade (2, 4) in the stator-rotor-stator arrangement is performed in an apparatus set to operating mode or non-operating mode.

29. The method according to any one of claims 22 to 28, wherein the supply material comprises hydrocarbons.

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