• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    fluidized bed reactor system. The invention relates to a fluidized bed reactor system consisting of at least two fluidized bed reactors and comprising a first and a second reactor (1, 2), each circulating fluidized bed being the line particle (7). ), comprising a particle separator (3) for transferring fluidized bed particles from the first to the second reactor, and a line of patches (17) exiting at the bottom of the second reactor (2) for the transfer fluidized bed flow back to the first reactor (1), characterized in that, at least in the second reactor (2), the reaction zones (9, 10, 22), separated by one or more flow controllers (18, 21) are provided and that the particle line (7) opens to the above second reactor (2) at least one flow controller (18).
    公开号:BR112012031619B1
    申请号:R112012031619-2
    申请日:2011-06-08
    公开日:2019-01-22
    发明作者:Tobias Pröll；Johannes Schmid；Christoph Pfeifer；Hermann Hofbauer
    申请人:Technische Universität Wien；
    IPC主号:
    专利说明:

    [001] The present invention relates to an improved fluidized bed reactor system consisting of at least two fluidized bed reactors provided in the form of circulating fluidized beds.
    STATE OF THE TECHNIQUE [002] Both in physical procedures and chemical reactions, involving a material exchange between two phases, large contact surfaces and complete mixing of the phases are as decisive as long residence times in contact or reaction zones corresponding to in order to obtain renovation and high yields. This applies equally to all phase transfers, regardless of whether the material exchange is to take place between solid, liquid or gaseous phases.
    [003] A possibility to extend contact times and increase contact surfaces or the number of contacts with different particles in the case of solid-liquid and solid-gas contacts is to conduct the two phases to stay in contact in countercurrent flow, such as it is, for example, described for spray columns, (sometimes with multiple stages) fluidized bed reactors, countercurrent contactors and columns packed by AWM Roes and W.P.M. Van Swaaij, Chem. Eng. J. 17, 81-89 (1979). In DE 10 2007 005 799 Al (published on April 24, 2008), the countercurrent principle is described as a specific example of combustion reactions. There, pyrolysis coke is used as a fuel and converted into a gas product that is rich in hydrogen and has a high value
    Petition 870180139065, of 10/08/2018, p. 14/79 calorific, in which bulk material serving as heat transfer medium is circulated by means of a bulk material conveyor and is conducted in a countercurrent flow to the gas flow containing the product gas.
    [004] Another possibility to increase the surface, which is also suggested by Roes and Van Swaaij (mentioned above), provides internal elements, which are well known in the field of packaged columns or columns of rotating discs.
    [005] An increase in residence times in contactors or reactors, for example, can also be achieved by providing flow controllers or restrictors to create zones of flow rates different from the phases to be brought into contact with each other. An example of a fluidized bed reactor like this is described in Kersten et al., Chem. Eng. I know. 58, 725-731 (2003). There, a circulating fluidized bed reactor for biomass gasification is described, which is divided into zones of different densities for both the circulating solid and the charger and for flue gases through a regular sequence of conical expansions in the elevator, in which solid particles and gases are conducted in the elevator in a co-current flow. A similar example for improving the flow profile in a fluidized bed reactor is described by J. Bu und J.-X. Zhu, Canadian J. Chem. Eng. 77, 26-34 (February 1999), where internal annular elements are provided in the elevator of a circulating fluidized bed reactor, having an effect similar to that of the conical expansions of Kersten and others (mentioned above).
    [006] For fluidized bed reactor systems in
    Petition 870180139065, of 10/08/2018, p. 15/79
    3/29 that two or more fluidized reactors communicate with each other, the measures indicated above to improve contact or material exchange between two phases, specifically between a solid and a liquid or gaseous phase, are unknown until now.
    This is certainly partly because of the fact that, in the past, particulate discharge from a second reactor had to be readily supplied into a first reactor as long as there were two fast fluidized bed reactors, particles in order to close the solid flow cycle.
    See, for example, EP 1,637,574 A1.
    Figures 1 and 2 therein show a fluidized bed reactor system consisting of two communicating reactors that can both be fast fluidized bed reactors.
    Since solids discharged from one reactor have to be loaded through the other reactor, the gas and solid flows from the two reactors have to flow in the current direction.
    EP figure 3
    1,637,574
    Al also shows a system consisting of two reactors communicating where a gas and a solid are brought into contact in the second reactor in countercurrent flow.
    However, the second reactor is a bubbling fluidized bed reactor without solid discharge to the reactor head. The reactor system according to figure 3 thus comprises only a fast fluidized bed reactor, in which in the particle recirculation into which, precisely, a bubbling fluidized bed reactor is inserted, through which the flow particle descends before being recycled inside the first reactor.
    [007]
    In contrast to this, the inventors of the present
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    4/29 subject matter presented a fluidized bed reactor system, in their previous orders AT A 1272/2007 and WO 2009/021258, where two fluidized bed reactors, that is, particle transport, fast communicating with each other the other are connected by means of a line of particles in their lower halves, preferably in their lower thirds or quarters, so that the solid particles circulating between the two reactors do not necessarily have to pass through two particle separators in the reactor heads. Instead, or in addition, the particles can be transferred directly (or via an optional third interposed reactor) from one reactor to the other in order to close the solids cycle. However, an improvement in the contact between the circulating solids and the feed treated in the reactor system would also be desirable in the new inventors' system.
    DISCLOSURE OF THE INVENTION [008] The present invention thus provides a fluidized bed reactor system consisting of at least two fluidized bed reactors, comprising a first and a second reactor, each being a circulating fluidized bed, a line of particles comprising a particle separator to transfer fluidized bed particles from the first to the second reactor, and a line of particles exiting in the lower half of the second reactor to transfer fluidized bed particles back to the first reactor, characterized in that, at least in the second reactor , reaction zones separated by one or more flow controllers are provided and the
    Petition 870180139065, of 10/08/2018, p. 17/79
    5/29 particles to transfer fluidized bed particles from the first to the second reactor open into the second reactor above at least one flow controller. [009] With this inventive interpretation of a fluidized bed reactor system comprising two fast fluidized bed reactors carrying particles, for the first time it is possible to combine the advantages of the countercurrent principle with those of flow profiles regulated by means of flow controllers , which results in better mixing, longer contact times and thus in general better contact between a circulating solid and phases to be brought into contact with it, regardless of whether solid, liquid or gaseous phases. In addition, a lower volume fluid flow is required to elevate the fluidized bed particles, i.e., to generate and maintain a fluidized bed, than without a flow controller. Among other things, all of this allows for a more economical operation of a fluidized bed reactor system.
    [0010]
    Dividing at least one reactor of the inventive fluidized bed reactor system into several reaction zones allows, for example, the conduct of different physical or chemical reactions;
    for example, a predetermined sequence of chemical reactions, in the individual reaction zones. In addition to generating a counterflow of particles from the first reactor and the flow between the fluids in the second reactor, an appropriate selection of the junction position of the particle line from the first to the second reactor allows to control the reactions taking place in the reaction zones.
    [0011] In this document, the term fluid means from
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    6/29 generally, liquids, gases and mixtures thereof, in which, for special applications of the inventive fluidized bed reactor system such as CLR (chemical cycle reform), CLC (chemical cycle combustion), coal gasification or biomass and more, fluids are preferably gases. Conversely, when there is no reference for specific applications where the use of fluids other than gases, it is technically impossible, gas in this document also represents the general term fluid.
    [0012] Because of the facts in which the particle line from the first to the second reactor opens into the second reactor above a lower flow controller and that below this junction a countercurrent is generated between particles descending in the second reactor and the upward fluid flow, there is at least one reaction zone where the countercurrent exerts its full effect. For example, if two flow controllers, that is, three reaction zones, are provided and said particle line opens into the second reactor in the central reaction zone, there is additionally a reaction zone, that is, the highest , in which the fluid and solids are in a co-current flow. On the other hand, if the fluid and solids are to flow in the countercurrent direction, the line of particles preferably enters above the highest flow controller.
    [0013] Depending on the intensity of the fluid flow in the second reactor and the characteristics of the particles circulating between the two reactors (ie specific weight, shape, surface characteristics, etc.), the particles
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    7/29 are dragged by the fluid flow over different extensions and are thus distributed in the various reaction zones over different extensions. This results in a controllable probability of the presence of particles in the individual reaction zones of the second reactor, so that lower reaction zones usually comprise a larger particle mass than in the higher zones. If the particles (also) serve as heat carriers, for example, in CLR applications, different amounts of heat are available for chemical or physical reactions in the various reaction zones of the second reactor, in the case of CLR reactors to reform the fuel in the reactor of fuel.
    [0014] If particles having different characteristics, for example, particles of different weights and / or shapes, are present in the system, an accumulation of particles of less weight or of larger surfaces (in the following collectively referred to simply as particles of lower weight, for simplicity's effect) can be achieved in higher reaction zones, while consequently heavier particles or particles with a lower surface / volume ratio (collectively referred to as higher weight particles below) accumulate in lower reaction zones . Thus, smaller weight particles are more often discharged into the head of the second reactor, whereas in the particle line to transfer fluidized bed particles back to the first reactor, preferably larger weight particles circulate. This means that, in addition to the counter current effect and the generation of several
    Petition 870180139065, of 10/08/2018, p. 20/79
    8/29 reaction zones, there is also a separation of particles present in the system. Different particles can be introduced specifically into the system and can also be formed in the system through physical or chemical reactions, for example, by abrasion or combustion (for example, fly ash).
    [0015] Flow controllers are not particularly limited and any constriction or expansion of the reactor cross section, deviation of the particulate flow or any combination thereof can be used. Thus, the scope of protection of the invention comprises zigzag paths of the reactor tube as well as the provision of various internal elements, for example, central or side deflectors, annular constrictions, etc., which can be provided at any angle in relation to the flow direction. The type of flow controller is mainly determined by the intended purpose of the respective fluidized bed reactor system and the used reactor wall material. For example, for CLR, CLC, gasification and other applications that require high temperatures, mainly refractory and other temperature resistant materials, for example, brick, concrete or graphite bricks are used as wall materials.
    [0016] The present invention also comprises modalities where not only the second reactor, but also the first optional reactor and / or additional reactors are equipped with flow controllers to define zones of different particle densities in them. In CLC and CLR applications, for example, where a metal oxide, which serves as
    Petition 870180139065, of 10/08/2018, p. 21/79
    9/29 a heat carrier and an oxidizing agent and circulates between the reactors, is regenerated (ie, reoxidized) in the first reactor (the air reactor), different dwell times can be adjusted for the present oxide particles to be oxidized at different heights or in zones of different oxygen densities, which can, together with an adequate selection of air flow, result in milder or more economical reactions.
    [0017] In preferred embodiments of the inventive fluidized bed reactor system, the second reactor has a particle feedback line with a particle separator, which opens into the second reactor below at least one flow controller provided in the second reactor and / or opens into the first reactor in the lower half of it. On the one hand, this requires that the particles recycled in the second reactor pass through at least one reaction zone located above the particle feedback line junction before being optionally discharged back into the reactor head and recycled again. On the other hand, when the particle feedback line of the second reactor opens into the first reactor in a position in the lower half of it, preferably in the third or fourth lower part of the same, the residence time of the particles in the first reactor is sufficiently long to get them to participate in reactions happening at this location. In the above example of a reactor system for CLR applications, this reaction is, for example, the reoxidation of the heat carrier / oxidizing agent circulating between the reactors. If the particle feedback line in the
    Petition 870180139065, of 10/08/2018, p. 22/79
    10/29 second reactor has a flow divider, both modalities can be implemented simultaneously.
    [0018] If a flow divider like this is present, part of the solid collected in the particle separator can also be recycled in the reactor system, and the other part can be discharged from the system, for example, to subject this solid part to a external regeneration treatment or because it has lost the desired particle size due to abrasion and must be replaced with suitable particle material.
    [0019] Additionally, one or both particle separators of the first and second reactors can be double or multiple stage separators. For example, in addition to a gravitational separator that directly recycles the solids (for example, of greater weight) separated therein into the second reactor, the particle separator of the second reactor can also comprise a centrifugal separator, for example, a cyclone, which recycles the particles (for example, of less weight) separated in it at a different location into the second reactor or into the first reactor or discharges them. Alternatively or additionally, a two-stage particle separator can be provided for the first reactor, in which two stages of lower weight and higher weight are collected and introduced into the second reactor at different times in order to increase their turnaround times. inside the second reactor.
    [0020] For the same reason, the two particle feedback lines from a two-stage particle separator in the second reactor can open inwards
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    11/29 of the second reactor at different heights, for example, above and below a flow controller, respectively. The inventive fluidized bed reactor system thus not only allows particles to be directed countercurrently to the fluid flow, but at the same time enables particles of different sizes to flow countercurrently, which can be especially advantageous in cases where chemical reactions in the reactor system they result in particles of different sizes, for example, in order to bring solid reaction products back into contact with the actual fluidized bed particles or to put them in contact for a longer period of time.
    [0021] In general, neither the design and functional principles of a particle separator in the inventive fluidized bed reactor system or its individual stages nor the destination of lines leading away from this are particularly limited as long as at least one line of particles drive from the first to the second reactor and open into the last above at least one flow controller. The particulate material accumulating in any other particle separators or in lines leading away from it can be recycled into the fluidized bed reactor system at any location or discharged from it if it serves the respective intended purpose of the reactor system.
    [0022] According to the present invention, all lines of particles can be provided with barriers for fluid or gas, that is, preferably they are fluidized, in order to prevent fluids, especially gases, from passing from one reactor to the other by because of different pressures.
    Petition 870180139065, of 10/08/2018, p. 24/79
    12/29
    Particle lines can be single runners, but belt or screw conveyors are also suitable. In preferred embodiments having fluidized lines, the most preferable gas barrier is a siphon, which is especially effective in preventing unwanted gas, but also solids, passage from one reactor into the other.
    [0023] Particularly preferred is a fluidized particle line for transferring fluidized bed particles back from the second to the first reactor, and even more preferably it is provided with a siphon. As mentioned earlier, this not only prevents unwanted material passages between the reactors, but also clogging the particle line, since in particularly preferred embodiments these lines of particles open up into the first reactor at small heights, which ensures that the inventive reactor systems work continuously.
    [0024] In a conventional way by itself, both reactors can be provided with staggered fluid inlets, for example, with several fluid inlets at different heights of the respective reactor, which favors the maintenance of the fluidized bed in the reactor. If staggered fluid inlets are provided in the first reactor, the lower fluid inlet can be replaced by a fluidized particle line to transfer fluidized bed particles from the second to the first reactor.
    [0025] In addition, in particular modalities, one or more additional reactors can be supplied in addition to the two
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    13/29 mentioned reactors, whose additional reactors can be mounted in any position within the inventive fluidized bed reactor system. For example, a third reactor can be operated in parallel with the first or second reactor so that the third reactor communicates exclusively with the second or the first reactor. Alternatively or additionally, a third reactor can - in both directions of the flow of circulating particles - be placed between the first and second reactors. This means that the particle flow from the first reactor can first be conducted into a third reactor before passing there to the second reactor, or the particle feedback from the second to the first reactor flows through a third reactor. In the latter case, a third reactor like this can be positioned on the particle line to transfer fluid bed particles from the second to the first reactor, or on a particle feedback line leading from the particle separator of the second reactor to the first reactor.
    Any combination of these modalities, that is, when adding several additional reactors, is possible.
    [0026] mode of operation of the third reactor and any additional reactors is not particularly limited. They can be operated as quick fluidized bed reactors, bubbling fluidized bed reactors or in any other way, as long as the advantageous effects of the inventive fluidized bed reactor system are not impaired.
    [0027] In the following, the present invention is
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    14/29 described in additional details with reference to specific modalities shown in the attached drawings.
    BRIEF DESCRIPTION OF THE DRAWINGS [0028]
    Figure 1 shows an embodiment of the inventive fluidized bed reactor system, comprising flow controllers only in the second reactor.
    [0029]
    The figure shows a modality of the inventive fluidized bed reactor system, comprising a different type of flow controller only in the second reactor.
    [0030]
    The figure shows a modality of the inventive fluidized bed reactor system, comprising flow controllers in both reactors, a third reactor interposed.
    [0031]
    Figure 4 shows a similar embodiment of the inventive fluidized bed reactor system as in Figure 3, but comprising two-stage particle separators.
    [0032]
    Figure 5 shows a similar embodiment of the inventive fluidized bed reactor system as in Figure 4, but comprising cross particle feedback lines.
    [0033]
    Figure 6 shows a detailed view of a reactor divided into reaction zones by flow controllers in an inventive fluidized bed reactor system.
    [0034]
    Figure 7 is a photograph of a reaction zone of an inventive fluidized bed reactor system.
    DETAILED DESCRIPTION OF THE INVENTION [0035]
    In general, the invention concerns
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    15/29 a fluidized bed reactor system consisting of at least two fluidized bed reactors, each being a circulating fluidized bed, in which at least one of the reactors is divided into separate reaction zones by means of one or more flow controllers flow. In at least some of the reaction zones, material flows to be reacted with each other are additionally directed countercurrently with each other, that is, a flow of solids is conducted countercurrently to a gas flow of reaction, and / or two streams of solids, for example, a solid serving as a reagent and another solid serving as a catalyst, are conducted countercurrent with each other.
    [0036] This type of flow management is, as mentioned above, based on the previous invention of the inventors of the present subject in question and described in AT A 1272/2007 and WO 2009/021258. Without the line of particles revealed therein to connect the two reactors and the (direct) feedback of the flow of particles from the second reactor to the first reactor, an implementation of the countercurrent principle would be technically impossible. Reaction zones may have been considered, but their effects are greatly enhanced by countercurrent material flows in them, so that all three elements of the present invention together have a synergistic effect.
    [0037] In the following, several preferred embodiments of the fluidized bed reactor system of the invention are described in more detail with reference to their modes of operation and with reference to the drawings, in which a CLC,
    Petition 870180139065, of 10/08/2018, p. 28/79
    Ie, combustion system by chemical cycles, is used for illustrative purposes. However, it is to be understood that the inventive fluidized bed reactor system is also suitable for any other physical or chemical reactions.
    [0038] CLC is a process of energy conversion theoretically without loss of efficiency, in which a fuel, for example, coal or natural gas, is burned, usually with the exclusion of air, in a fuel or combustion reactor by use of an oxygen carrier serving both as an oxidizing agent and as a catalyst, while the oxygen carrier is regenerated in a second reactor, that is, the air reactor. The oxygen charger / catalyst is usually a metal oxide that is reduced in the fuel reactor and reoxidated in the air reactor. During combustion, mainly CO2 and H2O are formed, of which CO2 can be obtained after water condensation.
    [0039] Figure 1 shows a preferred modality with the two fast fluidized reactors, that is, particle transport, 1 and 2. Solids discharged from the first reactor 1 are collected in a particle separator 3, while gas is discharged by middle of outlet 5. For the CLC example, the first reactor 1 is the air reactor, so that mainly N2 and O2 are discharged in 5, while the oxygen carrier, that is, for example, a metal oxide , is separated into 3 and introduced into the second reactor 2 by means of a particle line 7. The particle separator 3 is not particularly limited and, for example, can be a gravitational or a separator
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    17/29 centrifugal, preferably a cyclone. The particle line 7 is also not particularly limited and, for example, it can be a screw conveyor, a simple rail or the like. As shown by the black arrows in figure 1, it is preferably fluidized with an inert gas, so that for the gas barrier between the reactors a siphon can be used preferably, although any other gas barrier providing a sufficient pressure difference between the gas phases to be separated is also suitable, for example, fluidized gutters or the like.
    [0040]
    By selecting the position in which the particle line from the first reactor opens into the second reactor 2, we can control the extent to which the particles are taken countercurrently to the material flows in the second reactor, that is, gas or fluid flows or solids.
    Material (product) flows are marked with white arrows in all drawings.
    The figure shows a preferred mode where line 7 enters a very high position, above the highest flow controller, that is, in the highest reaction zone 10, which will be explained in more detail later. Hence, the particles descend into the fluidized bed of the second reactor 2, so that a flow of these particles in the countercurrent direction for the gas flow, and sometimes also for the flow of solids, in this reactor is guaranteed for most of your Height.
    [0041] Fluidized bed reactor 2, in the CLC example the fuel reactor, is also fluidized fast and
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    18/29 comprises a gas outlet 6, a particle separator 4 and a particle line or feedback line 8, which is also shown fluidized in the present example and so is preferably a siphon, although the particle separator 4 and the particle line 8 again are not particularly limited. In the example of figure 1, the particle line 8 opens into the second reactor 2 and thus recycles solids discharged from it. The position marked in figure 1, in which the feedback line 8 opens into the reactor 2, is at a relatively low height, which has the effect that most of the solids thus recycled rise again in the fluidized bed of the reactor (for example, ash particles that still contain a part of combustible material) and is thus conducted in the countercurrent direction for the particles introduced by the first reactor 1. The last particles pass through the reactor 2 in the countercurrent direction for the gas flow as well as for a flow of solids in it. A smaller part, for example, descends and, because of the introduction at a relatively low height, opens inwards.
    [0042] Although both reactors transport particles, unlike reactor 1, which is entirely particle transport, reactor 2 is implemented in a mode of transport only partially. This means that all the solids present in the fluidized bed of the reactor 1 are discharged and introduced into the second reactor 2, while the reactor 2 discharges only a small part of the solid particles present therein in the reactor head. In practice, for example, in CLC applications, this is a more or less small part, on the one hand because, if
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    19/29 possible, the total oxygen carrier mass must occur in cycles between the two reactors, and on the other hand because the solid fuel in reactor 2 has to be burned as completely as possible. In this example, the discharge from reactor 2 thus mainly consists of relatively thin components, for example, abrasion from the oxygen carrier or fly ash.
    However, in practical applications, there is always a certain part of coarser granular particles of greater weight in the discharge of the reactor 2 because all particles have a defined probability (even if somewhat low) of presence at any location within the system. reactor.
    [0043] Both reactors 1, 2 have two-part inlets 11-14, that is, the gas or fluidization fluid is introduced into the respective reactor at different times, which favors the maintenance of fluidized beds and makes it easier to introduce different fluids / gases in the respective reactor. In the case of CLC, for example, fresh air can be introduced into reactor 1 in 11, while in 13 a mixture of nitrogen and oxygen recycled from outlet 5 can be introduced. Because of the presence of a feed line 15, clean air can also be introduced at 11 and 13, while at 15 the flow of recycled gas is reintroduced, or pure oxygen or an additional fuel to heat the particles in reactor 1 can be entered in 15 (or 11 and / or 13). However, the respective purpose of a fluid supply line is not limited particularly in accordance with the present invention. [0044] A line of particles 17 connects the two
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    20/29 reactors, preferably at the lower ends, and recycle the flow of solids, in the example of CLC metal oxide, into the first reactor. Line 17 is similar to particle lines 7 and 8, that is, preferably it is fluidized and supplied in the form of a siphon. Because the exit point of the particle line 17 of the second reactor is positioned between inlets 12 and 14 it has the effect that the part of the gas (eg methane) introduced in 12 can contact the particle flow before the latter leaving reactor 2. The point of entry of the particle line 17 between the inputs 11 and 13 of reactor 1 has the effect that the particle flow is more evenly distributed in the reactor. Since the particle line 17 is fluidized, its junction can also replace the lower fluid inlet 11. Generally speaking, the relationship between particle flows and particle residence times in individual reactor sections can be well controlled by the appropriate selection of gas flows.
    [0045] The reactor 2 of figure 1 is divided, according to the invention, into seven reaction zones 10 by a total of six flow controllers 18, in whose reaction zones the solids contained in the system have different probabilities of presence and dwell times, which again are controllable through gas flows, but also through the type and design of flow controllers. Through the controllable intensity of the fluid or gas flow through the second reactor, the contact times between the reaction partners in the individual reaction zones are also controllable.
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    21/29 [0046] The presence of the fluidized bed particles, their global flow direction and fluidization in the reactors and their reaction zones are indicated by dashed lines in figure 1 and in the other attached drawings. This can be seen especially in figure 6 which shows a detailed view of a second reactor 2 divided into reaction zones by means of flow controllers in an inventive fluidized bed reactor system, but which does not show particle feedback for the second reactor. The type of flow controller 18, as mentioned earlier, is not particularly limited. Figure 1 and Figure 6 show modalities with constraints or narrowing (for example, annular) of the reactor cross section.
    [0047] In the preferred embodiment of figure 1, the power lines for reactor 2 are shown in 16 and 19, whose purpose of which is not particularly limited; in the CLC example, however, they are fuel supply lines. For example, at 16 a gaseous fuel such as methane can be introduced, while at 19 a feed consisting at least partially of solids, for example, coal, can be introduced.
    [0048] Seen as a whole, the inventive fluidized bed reactor system shown in figure 1 for an example of CLC allows (re) oxidizing and heating an oxygen carrier in the air reactor 1, which is then supplied via the particle line 7 to the highest reaction zone 10 of the fuel reactor 2, where it descends continuously within the fluidized bed and allows oxidation, that is,
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    22/29 combustion, of one or more fuels in the individual reaction zones, whose fuels can be introduced in 16 and / or 19. Then, the oxygen charger is supplied again to the air reactor 1 and regenerated. In the fuel reactor 2, solid combustion residues, but dispersed in a relatively fine way, for example, fly ash in coal combustion, can be collected in the particle separator 4 and recycled via the particle line 8 in the system, where they are placed in contact with the oxygen charger, which guarantees complete combustion of the fuel. At the same time, another fuel, for example, gaseous such as methane can be introduced, so that different amounts of different reaction partners are present in the individual reaction zones 10 which can have different temperatures and thus allow different liquid reactions. For example, these reactions create varying amounts of heat and solid reaction products of varying sizes, depending on the position of the respective reaction zone. In this way, in total, complete coverage of combustion reactions and increases in yields and process efficiency are obtained.
    [0049] Figure 2 shows an alternative preferred embodiment of the invention, where flow controllers 18 are provided in the form of zigzag paths or rails with additional internal elements being shown as angles. The operating mode of this system is the same as described in connection with figure 1.
    [0050] Figure 3 shows, in reactor 2, a combination of the designs of flow controllers 18 in figure 1 and
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    23/29 those of figure 2, that is, constraints of the reactor cross section as well as deviations, which can result in even longer residence times of the particles, for example, metal oxide oxygen carrier particles, in the zones of individual reaction. This modality also comprises continuous cross-sectional changes within the reaction zones of reactor 2. Additionally, in this modality, reactor 1 also comprises flow controllers 21 that divide it into several reaction zones 9. When used for CLC, for example, this can allow for a gradual and thus potentially smoother regeneration of the oxygen carrier in the air reactor 1, especially when fuel to heat the oxygen carrier is supplied to the air reactor via the supply line 15.
    [0051] Furthermore, between the second and the first reactor, that is, as seen in the direction of the particle flow circulating between the two reactors, a third reactor 20 is provided at the lower end of the reactor 2, which is shown as bubbling fluidized bed reactor or BFB and thus is not particulate transport. However, like any additional reactor, the third reactor is not limited to this and can be implemented in any position of the inventive fluidized bed reactor system and with any flow state, that is, stationary or transport, as a homogeneous fluidized bed. , bubbly, slow, turbulent or fast or with pneumatic transport (see Grace and Bi, 1997). From the third reactor 20, a line of particles 17 results in the reactor 1 to recycle the particles.
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    24/29 [0052] The stationary fluidized bed in the third reactor 20 contains mainly particles of greater weight, while the reactor 2 positioned above contains particles of less weight, or appropriate control of the fluid supply in 12 and 14 as well as corresponding sizing of the constraints 18 ensure that a certain part of particles of the same type remain stationary in reactor 20 while the rest are subjected to rapid fluidization in reactor 2. Likewise, particles circulating through all three reactors, that is, the global circulation of solids , may consist of particles of substantially the same or particles of different weights, i.e., of different fluidisability.
    [0053] Because of the low height of the exit point of the particle line 17 of the third reactor 20 and because of the aforementioned probability of presence, a greater or lesser part of the same particles as in reactor 20 is also present in reactor 1 , which strongly depends on the control of fluid flows in the three reactors and the intensity of the fluidization flow of the line
    17. Whether these form a stationary bed at the bottom of reactor 1 or are discharged completely back into the head depends on the intensity of the fluid flows, in this case at 11 and 13 and on line 17, as well as on the fluidisability of the particles. Corresponding fluidization and filling height of the fluidized bed particles can result in a fill level balance between the first and third reactors, which ensures continuous operation of the inventive fluidized bed reactor system.
    Petition 870180139065, of 10/08/2018, p. 37/79
    25/29 [0054] Referring again to an exemplary CLC process, supplying a fuel, for example, coal, via feed line 16 directly into the third reactor 20, containing a stationary fluidized bed, results in a first contact intensive between the coal and the oxygen carrier particles that cross the reactor 2 and the reactor 20 in the countercurrent direction for the gas flows in them and for the coal particles. After the first combustion phase, the reaction products formed from coal are more easily fluidizable and are increasingly thrown upwards into the reactor
    2, in reaction zones 10 where they have increasing contact with a new oxygen carrier. After being discharged into the reactor head 2, the particles are collected in the particle separator and via the particle line are recycled in one of the lower reaction zones of the reactor
    2. Hence, they are mostly transported back up into the fluidized bed of reactor 2 and again come in contact with the oxygen carrier.
    This favors the complete combustion of the fuel.
    [0055] Figure 4 shows another modality of the fluidized bed reactor system of figure 3, where the particle separators of the two reactors have additionally two stages, so that the reactor 1 comprises the two particle separators 3 and 23, and the reactor 2 comprises the two particle separators 4 and 24. Here, the two original particle separators 3 and 4 are indicated as gravitational separators. The separator 3 discharges particles collected in it inside
    Petition 870180139065, of 10/08/2018, p. 38/79
    26/29 of the particle line 7, from which they are supplied to the reactor 2 at the junction point 27, while the particle separator 4 recycles the particles directly into the reactor 2 at the head thereof. Both the second stages, that is, the particle separators 23 and 24, supply the particles collected in them to the second reactor via lines of particles 25 and 26, respectively. In the present case, both lines of particles result in the same reaction zone 22, that is, the lowest, of the second reactor 2. Below that, the third reactor 20 is located.
    [0056] Except in the modality of figure 3, higher weight particles that still contain a greater part of combustible components are, after being discharged into the reactor head 2, collected in the first particle separator 4 and recycled directly inside the reactor 2, for example, by simply allowing them to flow backwards. Lesser weight particles, for example, consisting mainly of ash, are collected in the second stage of separator 24 and recycled in the reactor 2 via particle line 26. The particles collected in the second stage 23 of the particle separator of the reactor 1, which are , for example, combustion products carried along it or oxygen carrier particles that have undergone abrasion and thus show greater fluidisability, are brought into contact, in the lower reaction zone 22 of reactor 2, with the fuel particles rising from the third reactor 20, with particles recycled via particle line 26, with oxygen carrier particles precipitating from above, and optionally with solid fuel particles supplied via feed line 19 that descend
    Petition 870180139065, of 10/08/2018, p. 39/79
    27/29 mainly in the fluidized bed of the fuel reactor. In this way, particles of less weight contained in the system also pass through reactor 2 in the countercurrent direction for particles of greater weight, which again favors complete reactions (combustion) happening in reactor 2.
    [0057] Furthermore, the reaction zones 10 positioned one above the other have different cross sections, which results in different fluidization states in them, which again is indicated with dashed lines.
    [0058] In addition, the inputs of the third reactor 20 are provided at other times than those in the mode of figure 3. In figure 4, the lower fluid supply line 12 opens to the bottom of the reactor 20, which favors the fluidization of the reactor's stationary fluidized bed. On the other hand, the outlet point of line 17 of reactor 20 is positioned at a relatively low height, that is, at 28.
    [0059] Figure 5 shows a modality similar to figure 4 with two-stage particle separators 3, 4, 23, 24 and a third reactor 20. The difference for figure 4 relates to recycling the particles collected in the two-stage particles 4, 24, the junction of the particle line 7 with reactor 2 as well as the position of the particle line 17.
    [0060] In the modality shown in figure 5, the first stage 4 of the particle separator of the reactor 1 does not supply the particles collected in it back to the reactor head, but, through a feedback line 8, back to a reaction zone 10 more
    Petition 870180139065, of 10/08/2018, p. 40/79
    28/29 low, which also opens the particle line 7 from the first reactor 1. When performing a CLC process, recycled solids from separator 4 to fuel reactor 2, which mainly consist of fuel particles, are thus placed in contact with a new oxygen carrier from the air reactor, which again favors its complete combustion.
    [0061] The lower weight particles collected in the second separator stage 24, on the other hand, are supplied directly into the first reactor, that is, the air reactor. This is especially useful for substantially residue-free combustion of the solid fuel (s) in the fuel reactor, so that the particles collected in separator stage 24 consist mainly of oxygen carrier, for example, products abrasion, which are then transferred to the air reactor for regeneration without going through the fuel reactor again.
    [0062] Finally, the line of particles 17 between the third and the first reactor opens into or out of the reactors, respectively, at their bottoms. The fluidization flow of line 17 as well as that of direct fluidization 11 thus allows to control the extent of the overall circulation, i.e., the part of particles moving from the third to the first reactor. In particular, the selection of appropriate fluidization conditions favors the development of a fill level balance between the first and third reactors.
    [0063] As mentioned previously, figure 6 shows a detailed view of a second reactor 2 divided
    Petition 870180139065, of 10/08/2018, p. 41/79
    29/29 in reaction zones within an inventive fluidized bed reactor system, but without recycling particles to the second reactor and with a single fluidization 12. The countercurrent principle between fluidized bed particles supplied in 27 and discharged in 28 and the fluid flow supplied at 12 and discharged at 6 as well as the fluidization of particles within reaction zones 10 are easily recognizable.
    [0064] Figure 7 is a detail photograph of a reaction zone of an inventive fluidized bed reactor between two flow controllers, which clearly shows the distribution of fluidized bed particles within the reaction zone.
    [0065] Consequently, the preceding examples, given for illustrative purposes only and not to be understood as a limitation, must sufficiently prove that the present invention provides an improved fluidized bed reactor system to perform physical or chemical reactions, in which reactions can be carried out faster, more completely, with higher yields and thus more economically than would be possible according to the state of the art.
    权利要求:
    Claims (6)
    [1]
    1. Process of operating a fluidized bed reactor system consisting of at least two fluidized bed reactors for carrying out chemical reactions, a first and a second reactor (1, 2), being operated as circulating fluidized beds by the introduction of fluid through at least one fluid inlet (11, 12) at the bottom of the respective reactor (1, 2) and / or immediately above said bottom to generate a fast fluidized particle bed and by transporting fluidized bed particles across a line of particles (7) comprising a particle separator (3) from the first to the second reactor, and by returning them through a line of drainage particles (17) located in the lower half of the second reactor (2) to the first reactor (1), and by returning them through a particle feedback line (8), which comprises a particle separator (4) from the second reactor (2), the operation process of a reactor system characterized by the fact that reaction zones (9, 10, 22) separated by one or more flow controllers (18, 21) in the form of constraints of the reactor cross section for carrying out the chemical reactions are provided at least in the second reactor (2), each being located above a flow controller (18, 21), and that the line of particles (7) opens into the second reactor (2) above at least one flow controller flow (18), so that particles in the reaction zones (10, 22) above any flow controller (18) that is located below the opening of said particle line (7) are transported in the flow of
    Petition 870180139065, of 10/08/2018, p. 43/79
    [2]
    2. Process according to claim 1, characterized by the fact that particles are introduced into the second reactor (2) through the aforementioned particle line (7) above a higher flow controller (18) provided in the second reactor ( 2), so that the particles
    in all areas of reaction (10, 22) of second reactor (2) are transported in the countercurrent flow to the flow in fluid. 3. Process, according The claim 1 or 2,
    characterized by the fact that the particle separator (3) and / or the particle separator (4) is / are two-stage particle separator (s), in order to collect lighter or heavier particles and introduce them into different heights in the second reactor.
    2/3 countercurrent for fluid flow; and wherein the particles located below at least one flow controller (18) which is supplied in the second reactor (2) are introduced into the second reactor (2) and / or in the lower half of the first reactor (1) through the said line particle feedback (8), so that a part of these particles in the second reactor (2) moves in the upward direction again and are then transported in the countercurrent flow to particles introduced from the first reactor (1) through the line particles (7).
    [3]
    3/3 chemical reactions carried out in the fluidized bed reactor system comprise the conversion of fuels.
    [4]
    4. Process according to claim 3, characterized by the fact that particles of different sizes are transported in countercurrent to each other while chemical reactions are carried out.
    [5]
    5. Process according to any one of claims 1 to 4, characterized by the fact that the
    Petition 870180139065, of 10/08/2018, p. 44/79
    [6]
    6. Process, according to claim 5, characterized by the fact that fuels are
    introduced between two reaction zones (9, 10, 22) and / or a zone of reaction more low (22) and / or one third reactor (20) brought in between the first and second
    reactors.
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    法律状态:
    2018-07-10| B07A| Technical examination (opinion): publication of technical examination (opinion)|
    2018-12-11| B09A| Decision: intention to grant|
    2019-01-22| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 08/06/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    2019-11-12| B16C| Correction of notification of the grant|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 08/06/2011, OBSERVADAS AS CONDICOES LEGAIS. (CO) REF. RPI 2507 DE 22/01/2019 QUANTO A QUALIFICACAO DO DEPOSITANTE. |
    优先权:
    申请号 | 申请日 | 专利标题
    US35398510P| true| 2010-06-11|2010-06-11|
    ATA964/2010|2010-06-11|
    AT0096410A|AT509586B8|2010-06-11|2010-06-11|IMPROVED SWITCH LAYER REACTOR SYSTEM|
    US61/353,985|2010-06-11|
    PCT/AT2011/000254|WO2011153568A1|2010-06-11|2011-06-08|Fluidized bed reactor system|
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