WO2023072415A1 - Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants - Google Patents

Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants Download PDF

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Publication number
WO2023072415A1
WO2023072415A1 PCT/EP2021/080274 EP2021080274W WO2023072415A1 WO 2023072415 A1 WO2023072415 A1 WO 2023072415A1 EP 2021080274 W EP2021080274 W EP 2021080274W WO 2023072415 A1 WO2023072415 A1 WO 2023072415A1
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Prior art keywords
fluidizing
reactor
reaction
solid particles
steam
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PCT/EP2021/080274
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English (en)
Inventor
Teemu Rosnell
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Sumitomo SHI FW Energia Oy
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Application filed by Sumitomo SHI FW Energia Oy filed Critical Sumitomo SHI FW Energia Oy
Priority to CN202180103893.0A priority Critical patent/CN118338956A/zh
Priority to EP21806998.7A priority patent/EP4426476A1/fr
Priority to AU2021471099A priority patent/AU2021471099A1/en
Priority to KR1020247015473A priority patent/KR20240089524A/ko
Priority to PCT/EP2021/080274 priority patent/WO2023072415A1/fr
Publication of WO2023072415A1 publication Critical patent/WO2023072415A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J15/00—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J16/00—Chemical processes in general for reacting liquids with non- particulate solids, e.g. sheet material; Apparatus specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/004—Sparger-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1881—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving downwards while fluidised
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium

Definitions

  • the present invention relates to a fluidized bed reactor for continuous generation of thermochemical heat energy. According to a preferred embodiment, by utilizing solid particles from reaction calcium oxide + steam -> calcium hydroxide (Ca(OH)2).
  • the present invention relates to corresponding method for continuous generation of thermochemical heat energy, advantageously, from reaction calcium oxide (CaO) + water (H2O) in gas phase (steam) -> calcium hydroxide (Ca(OH) 2 ).
  • the present invention relates also to corresponding system for storing and releasing heat energy based on the reaction and its reverse reaction.
  • Fossil fuels have been a convenient and widely available source of energy but due to environmental aspects interest towards alternative fuels and energy production has been increased. Therefore, fuels with low-carbon energy carriers, with high energy density, have been found to be an alternative to replace the multiple indispensable roles of fossil fuels, including for electrical and thermal power generation, for powering transportation fleets, and for global energy trade.
  • a reversible exothermic reaction such as CaO with water is considered one of the most promising reactions for high temperature thermal energy storage.
  • Metal fuels, as recyclable carriers of clean energy, are promising alternatives to fossilfuels in a future low carbon economy. Metals have high energy densities and metals are, therefore, fuels within many batteries, energetic materials, and propellants.
  • Metal fuels can be burned with air or reacted with water to release their chemical energy at a range of power generation scales.
  • the metal-oxide combustion products are solids that can be captured and then be recycled using zero- carbon electrolysis processes powered by clean energy, enabling metals to be used as recyclable zero-carbon solar fuels or electro fuels.
  • a key technological barrier to the increased use of metal fuel is the current lack of clean and efficient combustor/reactor/engine technologies to convert the chemical energy in metal fuels in to motive or electrical power (energy).
  • WO 2021/105467 discloses a system for energy storage comprising a fluidized bed apparatus with an energy storage material.
  • the energy storage material comprises at least one selected from CaO, Ca(OH)2, CaCO3, MgO, Mg(OH)2, MgCO3, BaO, Ba(OH)2, BaCO3, and metal hydrides such as MgH2.
  • the fluidized bed apparatus comprises at least one perforated separator, the perforated separator creates more than one fluidization compartments in the fluidized bed apparatus. This creates a plurality of fluidization zones in the fluidized bed apparatus. Such a setup provides the possibility of having different conditions in the different zones.
  • the perforated separator is at least partially foraminous.
  • a perforated separator is in one embodiment arranged horizontally so that an upper and a lower fluidization zone are created. In another embodiment several perforated separators are arranged to create a plurality of fluidization zones.
  • a perforated separator has the advantage of creating several fluidization zones where the conditions can be held differently. For instance, the temperature can be different. The process can be made more efficient if for instance a first preheating is followed by a second heating to a higher temperature.
  • the devices for introduction of pressurized fluid are not shown in the publication.
  • An object of the invention is to provide an improved fluidized bed reactor for generation of thermochemical heat energy in which the performance is considerably improved compared to the prior art solutions, the performance is especially improved in terms of reliable operation, runnability, yield and efficiency during use of the reactor. Also it is an object of the invention to achieve an industry scale reactor where the reaction can occur in a uniform manner. It is an object of the invention to provide an improved fluidized bed reactor for solid particles of alkaline earth metals or one of metals from a group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe), and zinc (Zn). Disclosure of the Invention
  • thermochemical heat energy by utilizing one of reaction:
  • each one of the fluidizing stages comprises a number of nozzles for fluidizing the solid particles with a reactive fluidizer, the oxidizer or the hydrating compound, to initiate and proceed with the reaction,
  • - fluidizing stages are provided with one or more heat exchangers for selectively recovering the heat released from the reaction
  • an outlet is arranged at the opposite end to the first end of the reactor chamber for exit of reaction material.
  • thermochemical heat energy by utilizing one of reaction:
  • the method comprises following steps:
  • reaction material is removed from the reaction chamber via outlet.
  • reaction material refers to the end material i.e. reaction product that will be removed from the reaction chamber via outlet.
  • end material i.e. reaction product that will be removed from the reaction chamber via outlet.
  • reaction material is calcium hydroxide (Ca(OH) 2 ).
  • the solid particle size may be in the range of 1-1000 pm or 1-500 pm, or 100-300 pm.
  • the solid particle size has an effect on both the reaction itself and on the fluidizability of the particles, the smaller the particle size, the faster is the reactivity and fluidizability.
  • the particle size may selected as needed and practical operational conditions.
  • non-reactive fluidizer may be introduced to the reactor in addition of introducing a reactive fluidizer, the oxidizer or hydrating compound.
  • Non-reactive fluidizer means in this case that it will not participate in the reaction.
  • non-reactive fluidizer may improve distribution of particles and so promote reaction while not chemically participating it.
  • air and/or oxygen-containing gas as non- reactive fluidizer may be introduced into a reactor chamber.
  • non-reactive fluidizer may be introduced at same vertical levels as the reactive fluidizer.
  • the reactor is provided with nozzles for introducing a mixture of reactive fluidizer and non-reactive fluidizer into the reactor chamber, either via same nozzles or the reactor is provided with separate nozzles for reactive fluidizer and non-reac- tive fluidizer.
  • a mixture of reactive fluidizer and non-reactive fluidizer are introduced into the chamber via nozzles, either via same nozzles as the reactive fluidizer or the reactor is provided with separate nozzles for reactive fluidizer and non-reactive fluidizer.
  • a nozzle means a device that produces substantially one directional flow over the nozzle.
  • each of the fluidizing nozzles being arranged in fluid communication with a source of reactive fluidizer so that reactive fluidizer will be introduced through nozzles, preferably, independently at each levels.
  • a non-reactive fluidizer such as inert gas, may be introduced into the reactor chamber.
  • a fluidized bed reactor for continuous generation of thermochemical heat energy by utilizing solid particles from reaction calcium oxide (CaO) + water (H2O) in gas phase (steam) -> calcium hydroxide (Ca(OH)2), the reactor comprising:
  • each one of the fluidizing stages comprises a number of steam nozzles for fluidizing CaO with steam to initiate and proceed with the reaction
  • - fluidizing stages are provided with one or more heat exchangers for selectively recovering the heat released from the solid material in the reaction,
  • an outlet is arranged at the opposite end to the first end of the reactor chamber (10) for exit of Ca(OH)2.
  • a method for continuous generation of thermochemical heat energy from reaction calcium oxide (CaO) +water (H2O) in gas phase (steam) -> calcium hydroxide (Ca(OH)2) comprises following steps:
  • reaction product Ca(OH)2 is removed from the reaction chamber via outlet.
  • thermochemical heat energy has been efficiently released from the feedstock and the reaction product is still in a dry particle or powderous form so that it is easy to store and it is relatively simple to regenerate in a reverse reaction back to the initial material, to alkaline earth metal or metal in elemental form or to alkaline earth metal or metal in oxidized form, such as Ca(OH)2 -> CaO.
  • the reaction of the temperature is a function of the steam partial pressure, below an equilibrium curve: e.g. at 100kPa (1bar) the equilibrium temperature is around 520C and if temperature is over 520C reaction turns into dehydration.
  • One advantage of the present reactor is that heat recovery with heat exchangers is improved because the reaction can take place uniformly in the reactor.
  • each one of the fluidizing stages comprises a number of steam nozzles for fluidizing CaO with steam to initiate and proceed with the reaction. It has been noted that an efficient thermochemical process is better to be conducted in several stages to have maximum efficiency and yield. However, the properties of calcium oxide and later mixture of calcium oxide / calcium hydroxide change during the process I reaction in such a way that the fluidizing properties are different.
  • the fluidizing stages are configured within one compartment to enable efficient flow and reaction of CaO I Ca(OH)2 in the reactor chamber.
  • the reactor chamber is free from division walls and/or compartments and/or perforated separators between fluidization stages.
  • the reactor may be designed to be free from compartments divided by perforated plates and/or division walls between the fluidization stages. It is thus possible to utilize advantageously the whole reactor chamber for promoting thermochemical reaction and recovering heat. It also prevents possible clogging problems or other accumulation of the material, meaning the feedstock, partially reacted material or the end product, in other words the reaction material.
  • one array of fluidization stage is arranged at a bottom portion of the reactor chamber so as to form a first fluidization stage and other arrays of fluidization stages are arranged at a vertical level higher than the first fluidization stage.
  • different arrays of fluidization stages can be arranged at different vertical levels. It is possible to utilize stages at different levels in a reactor chamber arranged vertically or in an inclined configuration of the reactor chamber.
  • different fluidization stages or different fluidizations levels may provide the following synergy and/or advantages: distribution of particles will be improved with fluidization while utilizing the fluidization agent as media for participating in reaction and forming end material, from the feedstock and fluidization agent, at the same time.
  • Fluidization agent may be ‘consumed’ and/or ‘captured’ in the reaction of forming end material.
  • feedstock material e.g. CaO
  • formed end product e.g. Ca(OH)2
  • fluidizing agent e.g. steam
  • the fluidizing agent may have different density than the feedstock and/or end product.
  • the reactor is circular in cross section and has its length greater than the width or diameter.
  • the fluidization and the following reaction can be done in an efficient manner and the length enables that the reactor may comprise two to five fluidizing stages in the reactor chamber, preferably 3 to 4 fluidizing stages. Further this enables the process efficiency to be adapted to the optimum, about all the input material is reacted to calcium hydroxide and no by-pass or spillover calcium oxide is flown to the outlet of the reactor.
  • the reactor is vertical having the inlet and outlet configured on vertical position relating to each other in the reactor chamber.
  • a vertical height of the reactor is greater than a horizontal width of the reactor.
  • the control parameters are input feed (mass flow), fluidizing steam velocity at nozzles of each stage, steam temperature and saturation (water content).
  • the steam temperature may be increased gradually, decreased gradually or stay the same from fluidizing stage to consequent fluidizing stage.
  • the steam velocity at steam nozzle may decrease or increase gradually from fluidizing stage to consequent fluidizing stage.
  • Nozzle sizes and/or shapes may vary in the fluidizing stage and/or fluidizing stages so as to provide advantageous fluidization and reaction.
  • the reactor is provided with a gas exit channel for exit of excess fluid- izer.
  • a system for storing and releasing heat energy based on reaction CaO + H2O -> Ca(OH)2 and Ca(OH)2 + heat -> CaO + H2O the system comprises the reactor as explained above for utilizing method disclosed above, and wherein the system further comprises a storage for CaO and a storage for Ca(OH)2, and a regeneration reactor for a process of returning Ca(OH)2 back to CaO, the system is utilized in releasing heat when needed and storing heat when available.
  • the heat generated in the above explained reaction e.g. CaO + H2O -> Ca(OH)2, and recovered by the heat exchangers may be utilized for example in district heating and/or for generating electricity.
  • the fluidizing stages are provided with one or more heat exchangers for selectively recovering the heat released from the reaction.
  • This term “selectively recovering” means here that the heat exchangers may be different to each other in actual design or operating conditions, to achieve the most efficient heat recovery for each of the locations within the reactor chamber.
  • part of the generated heat is utilized in maintaining the reaction, to heat the fluidizing agent, such as steam.
  • the steam introduced into the reactor chamber may be extracted from a main steam line of the reactor. There are several possible ways to arrange the heat exchangers.
  • an arrangement of different heat exchangers ordering could be the following: superheater, evaporator, economizer, as the first heat exchanger in the reactor chamber would most likely to be the hottest one.
  • the aim is in all of the embodiments that the temperature of the reaction material at the outlet is as low as possible so that all the heat generated in the reaction has been transferred to the heat exchangers.
  • the reaction at the inlet side of the reactor chamber may be promoted, as well as distribution of particles with fluidization.
  • fluidization and/or particle velocity may be maintained at desirable level and/or uniform which may prevent potential erosion issues, for instance if the fluidization would be conducted only at the bottom of the reactor chamber.
  • Nozzle sizes and/or shapes may vary in the fluidizing stage and/or fluidizing stages so as to provide advantageous fluidization and reaction.
  • the reactor volume may be advantageously optimized to achieve high intensity in energy releasing.
  • FIG. 1 illustrates a reactor according to an embodiment of the invention
  • Figure 2a and 2b illustrates cross sectional nozzle configurations according to embodiments of the invention
  • FIG. 3 illustrates a reactor according to still another embodiment of the invention
  • FIG. 4 illustrates a system according to an embodiment of the invention
  • Figure 5 illustrates a reactor according to an embodiment of the invention.
  • Figure 1 depicts schematically a fluidized bed reactor 1 for continuous generation of thermochemical heat energy by utilizing one of reaction:
  • each one of the fluidizing stages 3 comprises a number of nozzles 32 for fluidizing the solid particles with a reactive fluidizer, the oxidizer or the hydrating compound, to initiate and proceed with the reaction,
  • - fluidizing stages 3 are provided with one or more heat exchangers 4 for selectively recovering the heat released from the reaction,
  • an outlet 5 is arranged at the opposite end to the first end of the reactor chamber 10 for exit of reaction material.
  • the reactive fluidizer is introduced through the nozzles 32 of each of the fluidizing stages 3 so as to fluidizing solid particles with the reactive fluidizer. It is illustrated a number of nozzles for feeding a reactive fluidized for fluidizing solid particles. Thus, it renders possible to introduce the reactive fluidizer through nozzles at different levels in Fig. 1 at different vertical levels. In addition to feeding reactive fluidizer, it may be possible to feed also non-reac- tive fluidizer from the same nozzles or a mixture of reactive and non-reactive fluidizer from the same nozzles. Thus, fluidization as well as reaction at each fluidization stage 3 may be advantageously controlled.
  • the Fig 1 depicts schematically a fluidized bed reactor 1 for continuous generation of thermochemical heat energy by utilizing solid particles from reaction calcium oxide (CaO) + water (H2O) in gas phase (steam) -> calcium hydroxide (Ca(OH)2), the reactor 1 comprising:
  • each one of the fluidizing stages 3 comprises a number of steam nozzles 32 for fluidizing CaO with steam to initiate and proceed with the reaction
  • - fluidizing stages 3 are provided with one or more heat exchangers 4 for selectively recovering the heat released from the solid material in the reaction,
  • an outlet 5 is arranged at the opposite end to the first end of the reactor chamber 10 for exit of Ca(OH)2.
  • the feedstock material CaO is stored to a storage 6 and from there is it fed to the reactor 1 by suitable means such as a screw conveyor (not shown, nor are valves and other instrumentation shown in in Fig. 1).
  • suitable means such as a screw conveyor (not shown, nor are valves and other instrumentation shown in in Fig. 1).
  • the reaction material or end material is led to a storage 7.
  • the reactor 1 is vertical having the inlet 2 and outlet 5 configured on vertical position relating to each other in the reactor chamber 10. According to an embodiment shown in in Fig.
  • the inlet 2 for introducing solid particulate material is arranged at a top portion of the reactor chamber 10 and outlet 5 for discharging reacted material is arranged at a bottom portion of the reactor chamber 10 so being opposite end of the inlet 2.
  • Fig. 1 there are presented an array of five fluidizing stages 3 with nozzles 32 in configured in suitable pattern as schematically shown in Fig. 2a or Fig. 2b. Said pattern can be formed for example so that there are pipes 31 where the nozzles are attached at certain spacing.
  • fluidizing stages it means fluidizing levels which are arranged within a certain vertical distance from each other.
  • one fluidization stage comprises nozzles 32 for introducing reactive fluidizer substantially at one vertical level.
  • reactive fluidizer will be introduced through the nozzles 32 so as to fluidize solid particles and participate in the reaction.
  • Vertical distance between fluidizing stages or levels may be equally distributed, meaning a constant distance in vertical direction between each other. Accordingly, it is thus ensured proper fluidization velocities and dispersion of solid particles in the reactor chamber from bottom to top. Sizes and/or shapes of nozzles 32 may vary in the fluidizing stage and/or fluidizing stages so as to provide advantageous fluidization and reaction.
  • Pipes 31 forms a manifold for steam or some other suitable reactive flu- idizer or fluidizing agent, such as air or oxygen.
  • Pipes 31 cross-section may have a circular cross-section or rectangular cross-section to name a few preferable cross-sections.
  • the heat exchangers are arranged in a basic configuration, one heat exchanger 4 layer arranged per each fluidizing stage 3. However, it may be altered so that the number of heat exchangers 4 is greater than the number of fluidizing stages 3 or the number of heat exchangers 4 is smaller than the number of fluidizing stages 3.
  • One heat exchanger 4 comprises at least one heat exchanger inlet 41 and at least one heat exchanger outlet 42 for heat transfer media (water, steam, some other fluid) to transfer the heat from the reactor 1 .
  • the heat exchanger inlets 41 and outlets 42 may be grouped in a suitable way, they may in an embodiment be connected in series or in parallel and the origin of the fluid for the heat exchanger may be from any suitable source. Also the target for the heated fluid from the heat exchanger may be any suitable.
  • the actual configuration of heat exchangers is a matter of reactor or plant design, the inner walls may be formed of heat exchangers or the heat exchangers may be configured extending in a radial direction in to the reactor chamber 10 (as shown in Fig.
  • the heat exchangers may comprise tubes and may be configured to extent into the reactor chamber as tube bundles (not shown in figures). Since the reaction and heat recovery can take place uniformly in the reactor, temperature of particles to be discharged is lowered. This means that the heat is recovered by the heat exchangers 4.
  • FIGs 2a and 2b represent a horizontal cross-section of the reactor chamber of Figure 1 , there are schematically shown some possible configurations of nozzles 32 arranged on pipes 31 that forms a fluidizing stage 3. Through the nozzles reactive fluidizer is introduced into the reactor chamber 10. Through the nozzles also non-reactive fluidizer may be introduced into the reactor chamber 10. As all the figures of this disclosure are schematic, elements are not shown in scale and the relative dimensions are for illustrative purposes only. However, all the fluidizing stages 3 are configured within one compartment to enable efficient flow and reaction of CaO I Ca(OH)2 in the reactor chamber 10. Thus the pipes 31 shown in Fig. 2a and 2b are not forming a compartment for each fluidizing stage 3 but the material can pass the pipe 31 arrangement. Therefore, clogging of particles may be avoided or mitigated, and operational availability and efficiency are improved compared to known solutions. With the present configuration of the fluidization stages, or in other words, fluidization introduction stages, the reaction takes uniformly place in the reactor chamber.
  • Fig. 3 it is presented still an embodiment of the reactor 1 where the fluidizing stages 3 are arranged so that there is a center pipe 31 to function as a manifold for nozzles 32 in the central area of the reactor chamber 10 and then there are nozzles arranged on the walls of the reactor chamber 10.
  • the fluidizing effect is determined with suitable directioning of the nozzles 32 together with the velocity of the fluidizing media (steam, etc.).
  • the reactor 1 is circular in cross section perpendicular to a general flow direction and has its length greater than the width.
  • This feature has an effect on the reaction time in the reactor, suitably the length, diameter and number of stages are the parameters to be selected for design the reactor.
  • Other possible reactor cross section shapes are rectangular and polygonal such as hexagonal or octagonal.
  • Heat exchangers are not shown in Figs. 2b and 3 but may be arranged as in Fig. 1 that is between the fluidizing stages.
  • one fluidization stage 3 is defined by a vertical distance of nozzles 32 at different vertical levels.
  • Fig 4 it is presented schematically a system 100 for continuous storing and releasing thermochemical heat energy based on one of reaction by utilizing one of reaction:
  • the system comprises the reactor 1 and wherein the system 100 further comprises a storage 6 for feedstock and a storage 7 for end material, and a regeneration reactor 8 for a process of returning the end material back to feedstock, the system 100 is utilized in releasing heat when needed and storing heat when available.
  • This storing and releasing energy or charging I discharging energy can be performed in one location or the charging can be performed where the energy is available and then the charged material is transported to a location where the energy is discharged from the material in a reactor of the present disclosure.
  • FIG. 5 it is presented still an embodiment of a fluidized bed reactor (1) for continuous generation of thermochemical heat energy by utilizing one of reaction:
  • each one of the fluidizing stages 3 comprises a number of nozzles 32 for fluidizing the solid particles with a reactive fluidizer, the oxidizer or the hydrating compound, to initiate and proceed with the reaction,
  • - fluidizing stages 3 are provided with one or more heat exchangers 4 for selectively recovering the heat released from the reaction,
  • an outlet 5 is arranged at the opposite end to the first end of the reactor chamber 10 for exit of reaction material.
  • the solid particles are used as a feedstock to the process, first stored in a storage 6, the fed through inlet 2 to the reactor 1 and reactor chamber 10, then fluidized and the reaction is initiated and proceed.
  • the reactor may be provided with single nozzles 32, 32a for introducing a mixture of reactive fluidizer and non-reactive fluidizer into the reactor chamber, via same nozzles 32.
  • the reactor is provided with two rows of nozzles 32, 32a, i.e.
  • nozzles 32 for reactive fluidizer and nozzles 32a for non-reactive fluidizer may be particularly suitable for materials that require more effort in fluidizing, i.e. more dense solid particle materials or such.
  • a material (volume) input I output balance may be such that a separate gas exit channel 9 may be needed.
  • the gas exit channel may be equipped with a particle separator or similar to avoid the solid particles to escape from the reactor chamber through that route. In cases that the process requires that an amount of reactive fluidizer is exceeding the actual amount participating in the reaction, such gas exit channel may be needed also with reactors 1 having only single type fluidizer feed, i.e. nozzles 32 for reactive fluidizer.
  • steam introduced as reactive fluidizer temperature of the steam increases gradually, decreases gradually or stays the same from fluidizing stage 3 to consequent fluidizing stage 3.
  • the steam velocity at steam nozzle 32 decreases or increases gradually from fluidizing stage 3 to consequent fluidizing stage 3.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'Invention concerne un réacteur à lit fluidisé (1) pour la génération continue d'énergie thermique thermochimique au moyen de l'une des réactions suivantes : 1) des particules solides de métal alcalino-terreux ou d'un des métaux d'un groupe constitué du lithium (Li), du bore (B), du magnésium (Mg), de l'aluminium (Al), du silicium (Si), du fer (Fe) et du zinc (Zn), sous forme élémentaire + oxydant sous forme gazeuse ou de vapeur telle que la vapeur, l'air ou l'oxygène, ou 2) des particules solides de métal alcalino-terreux ou d'un des métaux d'un groupe constitué du lithium (Li), du bore (B), du magnésium (Mg), de l'aluminium (Al), du silicium (Si), du fer (Fe) et du zinc (Zn), sous forme oxydée + composé hydratant sous forme gazeuse ou de vapeur afin d'obtenir de l'hydroxyde, le réacteur (1) comprenant : - une chambre de réacteur (10), - une entrée (2) agencée à la première extrémité de la chambre de réacteur (10) pour introduire des particules solides dans le réacteur (1), - à l'intérieur de la chambre de réacteur (10) est agencé un réseau d'étages de fluidisation (3), chacun des étages de fluidisation (3) comprenant un certain nombre de buses (32) pour fluidiser les particules solides avec un agent de fluidisation réactif pour initier et poursuivre la réaction, - les étages de fluidisation (3) étant pourvus d'un ou de plusieurs échangeurs de chaleur (4) pour récupérer de manière sélective la chaleur dégagée par la réaction, - une sortie (5) étant agencée à l'extrémité opposée à la première extrémité de la cuve de réacteur (10) pour la sortie du matériau de réaction. L'invention concerne également un procédé et un système correspondants.
PCT/EP2021/080274 2021-11-01 2021-11-01 Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants WO2023072415A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CN202180103893.0A CN118338956A (zh) 2021-11-01 2021-11-01 用于连续生成热化学热能的流化床反应器及对应的方法和系统
EP21806998.7A EP4426476A1 (fr) 2021-11-01 2021-11-01 Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants
AU2021471099A AU2021471099A1 (en) 2021-11-01 2021-11-01 A fluidized bed reactor for continuous generation of thermochemical heat energy and corresponding method and system
KR1020247015473A KR20240089524A (ko) 2021-11-01 2021-11-01 열화학적 열에너지의 연속 생성을 위한 유동층 반응기 및 대응하는 방법 및 시스템
PCT/EP2021/080274 WO2023072415A1 (fr) 2021-11-01 2021-11-01 Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2021/080274 WO2023072415A1 (fr) 2021-11-01 2021-11-01 Réacteur à lit fluidisé pour la génération continue d'énergie thermique thermochimique et procédé et système correspondants

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WO2023072415A1 true WO2023072415A1 (fr) 2023-05-04

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EP (1) EP4426476A1 (fr)
KR (1) KR20240089524A (fr)
CN (1) CN118338956A (fr)
AU (1) AU2021471099A1 (fr)
WO (1) WO2023072415A1 (fr)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005118465A1 (fr) * 2004-06-04 2005-12-15 ETH Zürich Procede et appareil permettant de produire simultanement de l'hydrogene ou de l'ammoniac et des nanoparticules d'oxyde metallique
FR3004245A1 (fr) * 2013-04-09 2014-10-10 Commissariat Energie Atomique Systeme de stockage thermique par voie thermochimique
EP3453997A1 (fr) * 2017-09-06 2019-03-13 Nederlandse Organisatie voor toegepast- natuurwetenschappelijk onderzoek TNO Système de stockage d'énergie comprenant un réservoir de fluide de transfert de chaleur
WO2021105467A1 (fr) 2019-11-28 2021-06-03 Saltx Technology Ab Système et procédé de stockage d'énergie

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005118465A1 (fr) * 2004-06-04 2005-12-15 ETH Zürich Procede et appareil permettant de produire simultanement de l'hydrogene ou de l'ammoniac et des nanoparticules d'oxyde metallique
FR3004245A1 (fr) * 2013-04-09 2014-10-10 Commissariat Energie Atomique Systeme de stockage thermique par voie thermochimique
EP3453997A1 (fr) * 2017-09-06 2019-03-13 Nederlandse Organisatie voor toegepast- natuurwetenschappelijk onderzoek TNO Système de stockage d'énergie comprenant un réservoir de fluide de transfert de chaleur
WO2021105467A1 (fr) 2019-11-28 2021-06-03 Saltx Technology Ab Système et procédé de stockage d'énergie

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CN118338956A (zh) 2024-07-12
KR20240089524A (ko) 2024-06-20
EP4426476A1 (fr) 2024-09-11
AU2021471099A1 (en) 2024-05-23

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