CN118338956A

CN118338956A - Fluidized bed reactor for continuously generating thermochemical heat energy and corresponding method and system

Info

Publication number: CN118338956A
Application number: CN202180103893.0A
Authority: CN
Inventors: T·罗斯内尔
Original assignee: Sumitomo Heavy Machinery Fuhui Energy Co ltd
Current assignee: Sumitomo Heavy Machinery Fuhui Energy Co ltd
Filing date: 2021-11-01
Publication date: 2024-07-12

Abstract

The invention relates to a fluidized bed reactor (1) for continuously generating thermochemical thermal energy by using one of the following reactions: 1) Alkaline earth metals in elemental form or solid particles of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) plus an oxidizing agent in gaseous or vapor form such as steam, air or oxygen, or 2) alkaline earth metals in oxidized form or solid particles of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) plus a hydrated compound in gaseous or vapor form to obtain hydroxides, the reactor (1) comprising: -a reaction chamber (10), -an inlet (2) arranged at a first end of the reaction chamber (10) for feeding solid particles into the reactor (1), -an array of fluidization stages (3) arranged inside the reaction chamber (10), wherein each of the fluidization stages (3) comprises a plurality of nozzles (32) for fluidizing the solid particles with a reactive fluidizing agent for initiating and carrying out the reaction, -the fluidization stages (3) are provided with one or more heat exchangers (4) for selectively recovering heat released from the reaction, -an outlet (5) is arranged at the opposite end of the first end of the reaction chamber (10) for discharging the reaction material. The invention also relates to a corresponding method and system.

Description

Fluidized bed reactor for continuously generating thermochemical heat energy and corresponding method and system

Technical Field

The present invention relates to a fluidized bed reactor for continuously generating thermochemical heat energy. According to a preferred embodiment, the solid particles are obtained by utilizing a reaction from calcium oxide + steam- > calcium hydroxide (Ca (OH) ₂).

The present invention relates to a corresponding process for the continuous production of thermochemical thermal energy advantageously from the reaction of calcium oxide (CaO) + water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂).

The invention also relates to a corresponding system for storing and releasing thermal energy based on this reaction and its inverse.

Background

Fossil fuels have been a convenient and widely available source of energy, but interest in alternative fuels and energy generation has increased due to environmental factors. Thus, fuels with low carbon energy carriers of high energy density have been found to be an indispensable alternative to fossil fuels for a variety of purposes including use in power generation and thermal power generation, powering transportation fleets, and for global energy commerce. Reversible exothermic reactions such as CaO with water are considered to be one of the most promising reactions for high temperature heat energy storage. Metal fuels as recoverable carriers of clean energy are expected to be alternatives to fossil fuels in the future in low carbon economy. Metals have high energy densities, and thus metals are fuels in many batteries, energetic materials, and propellants. The metal fuel may be combusted with air or reacted with water to release its chemical energy at a range of power generation scales. The metal oxide combustion products are solids that can be captured and then recovered using a zero carbon electrolysis process driven by a clean energy source, enabling the metal to be used as a recoverable zero carbon solar fuel or electrical fuel. One key technical hurdle to the increased use of metal fuels is the current lack of clean and efficient burner/reactor/engine technology to convert chemical energy in metal fuels into motive or electrical power (energy).

WO 2021/105467 discloses a system for energy storage comprising a fluid bed apparatus with energy storage material. The energy storage material includes 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 MgH ₂. In one embodiment, the fluidized bed apparatus comprises at least one porous partition that creates more than one fluidization compartment in the fluidized bed apparatus. This creates a plurality of fluidization areas in the fluidized bed apparatus. Such an arrangement provides the possibility of having different conditions in different areas. The porous separator is at least partially porous. In one embodiment, the porous partition is arranged horizontally, creating upper and lower fluidization regions. In another embodiment, several porous partitions are arranged to create multiple fluidization regions. The porous partition has the advantage of creating several fluidization areas in which different conditions can be maintained. For example, the temperatures may be different. The process may become more efficient if, for example, the first preheating is followed by a second heating to a higher temperature. The means for introducing the pressurized fluid are not shown in this publication.

It is an object of the present invention to provide an improved fluidized bed reactor for the generation of thermochemical heat energy, wherein the performance is significantly improved compared to prior art solutions, in particular in terms of reliable operation, operability, yield and efficiency during use of the reactor. In addition, it is an object of the present invention to achieve a technical grade reactor in which the reaction can take place in a uniform manner. The object of the present invention is to provide an improved fluidized bed reactor for solid particles of alkaline earth metals or one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn).

Disclosure of Invention

The objects of the invention may be substantially met as is disclosed in the independent claims and other claims describing further details of the different embodiments of the invention.

According to an embodiment, a fluidized bed reactor is provided for continuously generating thermochemical heat energy by utilizing one of the following reactions:

1) Alkaline earth metals in elemental form or solid particles of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) plus oxidizing agents in gaseous or vaporous form, such as steam or oxygen-containing gases or vapors, or

2) Alkaline earth metals in oxidized form or solid particles of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) plus hydrated compounds in gaseous or vapor form to obtain hydroxides,

The reactor comprises:

The reaction chamber is provided with a plurality of reaction chambers,

An inlet arranged to a first end of the reaction chamber for feeding solid particles into the reactor,

An array of fluidization stages is arranged inside the reaction chamber, wherein each of the fluidization stages comprises a plurality of nozzles for fluidizing solid particles with a reactive fluidizing agent, oxidizing agent or hydrating compound to initiate and carry out the reaction,

The fluidization stage is provided with one or more heat exchangers for selectively recovering the heat released from the reaction,

An outlet is arranged at the opposite end of the first end of the reaction chamber for discharging the reaction material.

According to an embodiment, a method for continuously generating thermochemical thermal energy by utilizing one of the following reactions is provided:

The method comprises the following steps:

feeding a feedstock of solid particles into the reaction chamber at a first end of the reaction chamber,

Fluidizing the solid particles with a fluidizing jet of a first fluidizing stage to initiate a reaction,

A heat exchanger for transferring the generated heat to the reaction chamber,

Continuing the feed of the feedstock from the first end of the reaction chamber forces the mixture of feedstock/partially reacted material to move to a subsequent fluidization stage where fluidization of the mixture with the fluidization jet continues and the released heat is transferred by the heat exchanger at this fluidization stage, as fluidization continues the mixture composition becomes more final material and after the last fluidization stage the mixture contains only a small proportion of feedstock, the yield of the reaction being controlled by the fluidization stream temperature, saturation and flow rate in each fluidization stage,

-Removing the reaction material from the reaction chamber via the outlet.

For clarification purposes only, the term reaction material refers to the final material, i.e., the reaction product that is to be removed from the reaction chamber via the outlet. For example, in the case where calcium oxide (CaO) +water in a gas phase (H ₂ O) (i.e., steam) is reacted, the reaction material is calcium hydroxide (Ca (OH) ₂).

According to an embodiment, when one of the disclosed metals is used as solid particles to be introduced into the reaction chamber, and when the fluidizing agent is an oxygen-containing gas, a combustible condition occurs in the reaction chamber. Generally, the use of metal powder with a staged fluidization reaction chamber will create a flammable environment as the metal will oxidize.

Since the general reaction, reactor and process disclosed above are applicable to several solid particulate or powdery materials, the invention is explained in more detail herein in connection with one of the preferred embodiments, this reaction is calcium oxide (CaO) +water in the gas phase (H ₂ O) (i.e. steam) - > calcium hydroxide (Ca (OH) ₂), as this is one of the most economically viable alternatives to achieve this. Another preferred embodiment is with magnesium: mgO+H ₂O→Mg(OH)₂ other disclosed materials can also be used: lithium (Li), boron (B), aluminum (Al), silicon (Si), iron (Fe), and zinc (Zn). In the following disclosure, even though the process is disclosed as a reaction using CaO/Ca (OH) ₂, the process and reactor are directly applicable to other disclosed materials: alkaline earth metals or one of metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn).

According to embodiments, the solid particle size may be in the range of 1-1000 μm or 1-500 μm or 100-300 μm. The solid particle size has an effect on both the reaction itself and the fluidizability of the particles, the smaller the particle size the faster the reactivity and fluidizability. The particle size may be selected as desired and practical operating conditions in order to achieve the desired controllability.

According to embodiments of the present invention, a non-reactive fluidizing agent may be introduced into the reactor in addition to the reactive fluidizing agent, oxidizing agent, or hydrated compound. The non-reactive fluidizer in this case means that it does not participate in the reaction. Advantageously, the non-reactive fluidizer may improve the distribution of the particles and thus promote the reaction while not chemically participating in the reaction. According to an embodiment of the present invention, in the case of calcium oxide (CaO) +water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂), where steam is a reactive fluidizing agent, air and/or an oxygen-containing gas as a non-reactive fluidizing agent may be introduced into the reaction chamber. According to embodiments of the present invention, the non-reactive fluidizing agent may be introduced at the same vertical level as the reactive fluidizing agent. According to an embodiment of the invention, the reactor is provided with nozzles for introducing a mixture of reactive and non-reactive fluidising agents into the reaction chamber, either via the same nozzle, or with separate nozzles for reactive and non-reactive fluidising agents. Thus, the mixture of reactive and non-reactive fluidising agent is introduced into the chamber via a nozzle, or via the same nozzle as the reactive fluidising agent, or the reactor is provided with separate nozzles for the reactive fluidising agent and the non-reactive fluidising agent. Here, a nozzle means a device that generates a substantially unidirectional flow over the nozzle. Thus, each of the fluidization nozzles is arranged in fluid communication with a source of reactive fluidization agent such that the reactive fluidization agent will be introduced through the nozzle, preferably independently at each elevation. According to an embodiment of the present invention, especially in the case of solid particles of one of metals of the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn), a non-reactive fluidizing agent such as an inert gas may be introduced into the reaction chamber.

According to an embodiment, when CaO is introduced and the fluidizing agent is steam, calcium hydroxide is formed and no combustion occurs.

According to an embodiment of the present invention, there is provided a fluidized bed reactor for continuously generating thermochemical thermal energy by utilizing solid particles from the reaction of calcium oxide (CaO) +water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂),

The reactor comprises:

The reaction chamber is provided with a plurality of reaction chambers,

An inlet arranged to a first end of the reaction chamber for feeding solid particles of CaO into the reactor,

An array of fluidization stages is arranged inside the reaction chamber, wherein each of the fluidization stages comprises a plurality of steam nozzles for fluidizing CaO with steam to initiate and carry out the reaction,

The fluidization stage is 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 of the first end of the reaction chamber (10) for discharging Ca (OH) ₂.

According to an embodiment of the invention, a method for continuously generating thermochemical heat energy from the reaction of calcium oxide (CaO) + water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂), the method comprising the steps of:

feeding solid particles of CaO into the reaction chamber at a first end of the reaction chamber,

Fluidizing CaO with a steam jet of a first fluidizing stage to initiate a reaction,

A heat exchanger for transferring the generated heat to the reaction chamber,

Continuing the feed of CaO raw material from the first end of the reaction chamber forces the partially reacted CaO/Ca (OH) ₂ mixture to move to a subsequent fluidization stage where fluidization of the mixture with steam jet continues and the heat released is transferred by a heat exchanger, as fluidization continues, the CaO/Ca (OH) ₂ mixture composition becomes more Ca (OH) ₂ and after the last fluidization stage the mixture contains Ca (OH) ₂ with only a small proportion of CaO, the yield of the reaction being controlled by the steam temperature, saturation and flow rate in each of the fluidization stages,

-Removing the reaction product Ca (OH) ₂ from the reaction chamber via the outlet.

This provides an effect by which thermochemical heat energy has been efficiently released from the feedstock and the reaction product is still in dry particulate or powder form, thus easy to store, and relatively simple to regenerate back to the starting material, alkaline earth metal or metal in elemental form or alkaline earth metal or metal in oxidized form, such as Ca (OH) ₂ - > CaO, in the reverse reaction. Thus, the performance of the reactors, methods, and systems for continuously producing thermochemical heat energy is significantly improved. The present invention ensures proper fluidization velocity and dispersion of solid particles inside the reactor from bottom to top. The temperature of the reaction is a function of the partial pressure of steam, below the equilibrium curve: for example, at 100kPa (1 bar) the equilibrium temperature is about 520 ℃, and if the temperature exceeds 520 ℃, the reaction becomes dehydrated. An advantage of the present reactor is improved heat recovery with a heat exchanger, as the reaction can take place uniformly in the reactor.

According to this embodiment, an array of fluidization stages is arranged inside the reaction chamber, wherein each of the fluidization stages comprises a plurality of steam nozzles for fluidizing CaO with steam to initiate and carry out the reaction. It has been noted that efficient thermochemical processes are best performed in several stages to have the highest efficiency and yield. However, the properties of the calcium oxide and the subsequent calcium oxide/hydroxide mixture change during the process/reaction in such a way that the fluidization properties are different. Thus, the feed of CaO continuing from the first end of the reaction chamber forces the partially reacted CaO/Ca (OH) ₂ mixture to move to the subsequent fluidization stage where fluidization of the mixture with the steam jet continues and the heat released is transferred by the heat exchanger where the CaO/Ca (OH) ₂ mixture composition becomes more Ca (OH) ₂ as fluidization continues and after the last fluidization stage the mixture contains Ca (OH) ₂ with only a small proportion of CaO. According to an embodiment, the fluidization stage is arranged in a compartment so as to enable efficient flow and reaction of CaO/Ca (OH) ₂ in the reaction chamber. In the prior art document WO 2021/105467 it is disclosed that the reaction is carried out in several compartments separated by a perforated or porous partition divided in the vertical direction. In theory, the compartments may also be arranged in a horizontal direction. However, in this prior art document, the examples are presented on a laboratory scale with a reactor volume of about 600ml. Since the present invention is intended for industrial scale operations and megawatt power capacities, the reactor volume will be counted from cubic meters to hundreds of cubic meters, the inventors have found that there may be potential plugging problems in the partition and that it would be better to simplify the reactor in a manner that would not require a partition or compartment. This has a considerable impact on the operability and operation of the reactor in continuous use, as the blockage will require the reactor to be shut down and cooled for several days until the blocked material is cleared.

According to an embodiment of the invention, the reaction chamber is free of partition walls and/or compartments and/or porous partitions between the fluidization stages. The effect of this feature is that an array of fluidization stages are arranged inside the reaction chamber, wherein each of the fluidization stages comprises a plurality of nozzles for fluidizing solid particles with a reactive fluidizing agent to initiate and conduct the reaction, and the reactor can be designed without compartments separated between the fluidization stages by perforated plates and/or dividing walls. Thus, it is possible to advantageously utilize the entire reaction chamber to facilitate thermochemical reactions and to recover heat. It also prevents possible clogging problems or other accumulation of material (i.e. raw materials, partially reacted material or end products, in other words reactive materials).

According to an embodiment of the invention, one array of fluidization stages is arranged at the bottom portion of the reaction chamber to form a first fluidization stage, and the other arrays of fluidization stages are arranged at a vertical height above the first fluidization stage. Advantageously, different arrays of fluidization stages may be arranged at different vertical heights. It is possible to utilize stages in vertically arranged reaction chambers or at different heights of the inclined configuration of the reaction chambers. Advantageously, different fluidization levels or different fluidization heights may provide the following synergy and/or advantages: the distribution of the particles will be improved by fluidization while utilizing the fluidizing agent as a medium for participating in the reaction and while forming the final material from the raw material and the fluidizing agent. In the reaction to form the final material, the fluidizer may be "consumed" and/or "captured". It should be noted that the feedstock material (e.g., caO) may have a density different from the final product (e.g., ca (OH) ₂) formed. Furthermore, the fluidization agent (e.g., steam) may have a different density than the feedstock and/or the final product.

According to an embodiment, the reactor is circular in cross-section and has a length greater than a width or diameter. Fluidization and subsequent reactions can be carried out in an efficient manner and the length is such that the reactor can comprise 2 to 5 fluidization stages, preferably 3 to 4 fluidization stages, in the reaction chamber. Furthermore, this allows the process efficiency to be adapted to optimum, with almost all of the input material reacting to form calcium hydroxide, and no by-pass or overflow calcium oxide flowing to the outlet of the reactor.

According to an embodiment, the reactor is vertical, having an inlet and an outlet arranged in a vertical position relative to each other in the reaction chamber. Preferably, in a vertical reactor configuration, the vertical height of the reactor is greater than the horizontal width of the reactor. With this vertical configuration it is possible to control the material flow and simultaneous reaction such that the control parameters are the input feed (mass flow), the fluidization steam velocity at the nozzles of each stage, the steam temperature and the saturation (water content). Still according to an embodiment, the steam temperature may gradually rise, gradually fall, or remain unchanged from the fluidization stage to the subsequent fluidization stage. According to an embodiment, the steam velocity at the steam nozzle may gradually decrease or increase from the fluidization stage to the subsequent fluidization stage. The nozzle size and/or shape may be varied in one and/or more fluidization stages to provide advantageous fluidization and reaction. Still according to an embodiment, the reactor is provided with a gas outlet channel for discharging excess fluidization agent.

According to an embodiment, a system for storing and releasing thermal energy based on the reaction of cao+h ₂O->Ca(OH)₂ and Ca (OH) ₂ +thermal- > cao+h ₂ O is provided, the system comprising a reactor as explained above for the use of the method disclosed above, and wherein the system further comprises a reservoir for CaO and a reservoir for Ca (OH) ₂, and a regeneration reactor for the process of bringing Ca (OH) ₂ back to CaO, the system for releasing thermal energy when needed and storing thermal energy when available.

The heat generated in the reaction explained above (e.g., cao+h ₂O->Ca(OH)₂) and recovered by the heat exchanger may be used, for example, for district heating and/or for power generation. The fluidization stage is provided with one or more heat exchangers for selectively recovering the heat released from the reaction. The term "selectively recovered" means herein that the heat exchangers may be different from each other under actual design or operating conditions in order to achieve the most efficient heat recovery for each location within the reaction chamber. Preferably, a portion of the heat generated is used to maintain the reaction to heat a fluidizing agent such as steam. In addition, the steam introduced into the reaction chamber may be extracted from the main steam line of the reactor. There are several possible ways to arrange the heat exchanger. For example, the order of arrangement of the different heat exchangers may be as follows: superheater, evaporator, economizer, since the first heat exchanger in the reaction chamber is most likely the hottest heat exchanger. The aim is in all 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 exchanger.

Advantageously, due to the fluidization stage, the reaction at the inlet side of the reaction chamber, as well as the distribution of the fluidization particles, can be promoted. Advantageously, fluidization and/or particle velocity may be maintained at a desired level and/or uniform, which may prevent potential erosion problems, for example, if fluidization is to be performed only at the bottom of the reaction chamber. The nozzle size and/or shape may be varied in one and/or more fluidization stages to provide advantageous fluidization and reaction. By means of staged fluidization, the reactor volume can be advantageously optimized to achieve high intensity in energy release.

The exemplary embodiments of the invention presented in this patent application should not be interpreted as limiting the applicability of the appended claims. The verb "comprise" is used in this patent application as an open limitation that does not exclude the presence of features not yet described. The features recited in the dependent claims are freely combinable with each other unless explicitly stated otherwise. The novel features believed characteristic of the invention are set forth in the appended claims.

Drawings

Hereinafter, the present invention will be described with reference to the accompanying exemplary schematic drawings, in which:

figure 1 illustrates a reactor according to an embodiment of the invention,

Figures 2a and 2b illustrate a cross-sectional nozzle configuration according to an embodiment of the invention,

Figure 3 illustrates a reactor according to yet another embodiment of the invention,

Figure 4 illustrates a system according to an embodiment of the invention,

Fig. 5 illustrates a reactor according to an embodiment of the present invention.

Detailed Description

Fig. 1 schematically depicts a fluidized bed reactor 1, which fluidized bed reactor 1 continuously generates thermochemical heat energy by utilizing one of the following reactions:

1) Alkaline earth metals in elemental form or solid particles of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) plus an oxidizing agent in gaseous or vaporous form such as steam, air or oxygen, or

The reactor 1 comprises:

the reaction chamber (10) is provided with a chamber,

An inlet 2 arranged to a first end of the reaction chamber 10 for feeding solid particles into the reactor 1,

An array of fluidization stages 3 is arranged inside the reaction chamber 10, wherein each of the fluidization stages 3 comprises a plurality of nozzles 32 for fluidizing solid particles with a reactive fluidizing agent, oxidizing agent or a hydration compound to initiate and carry out the reaction,

The fluidization stage 3 is provided with one or more heat exchangers 4 for selectively recovering the heat released from the reaction,

At the opposite end to the first end of the reaction chamber 10, an outlet 5 is arranged for discharging the reaction material.

In other words, the reactive fluidizer is introduced through the nozzle 32 of each of the fluidization stages 3 in order to fluidize the solid particles with the reactive fluidizer. A number of nozzles for feeding a reactive fluidizing agent for fluidizing solid particles are illustrated. This therefore makes it possible to introduce the reactive fluidizer at different vertical heights through nozzles at different heights in fig. 1. In addition to feeding the reactive fluidizer, it is also possible to feed the non-reactive fluidizer from the same nozzle or to feed a mixture of reactive and non-reactive fluidizers from the same nozzle. Thus, fluidization and reaction at each fluidization stage 3 can be advantageously controlled.

According to a preferred embodiment, fig. 1 schematically depicts a fluidized bed reactor 1 for continuously generating thermochemical thermal energy by utilizing solid particles from the reaction of calcium oxide (CaO) +water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂),

The reactor 1 comprises:

the reaction chamber (10) is provided with a chamber,

An inlet 2, arranged to a first end of the reaction chamber 10, for feeding solid particles of CaO into the reactor 1,

An array of fluidization stages 3 is arranged inside the reaction chamber 10, wherein each of the fluidization stages 3 comprises a plurality of steam nozzles 32 for fluidizing CaO with steam to initiate and carry out the reaction,

The fluidization stage 3 is provided with one or more heat exchangers 4 for selectively recovering the heat released from the solid materials in the reaction,

An outlet 5 is arranged at the opposite end of the first end of the reaction chamber 10 for discharging Ca (OH) ₂. In addition to the reactor 1 itself, an embodiment is presented in fig. 1 in which the raw material CaO is stored to a reservoir 6 and fed therefrom to the reactor 1 by means of suitable devices such as screw conveyors (not shown in fig. 1, nor valves and other instrumentation). After the reactor 1, the reaction material or the final material is led to a reservoir 7. The reactor 1 is vertical with an inlet 2 and an outlet 5 arranged in a vertical position relative to each other in a reaction chamber 10. According to the embodiment shown in fig. 1, the inlet 2 for introducing solid particulate material is arranged at the top portion of the reaction chamber 10, and the outlet 5 for discharging reacted material is arranged at the bottom portion of the reaction chamber 10, thus being the opposite end of the inlet 2. In fig. 1, an array of five fluidization stages 3 is presented, wherein the nozzles 32 are arranged in a suitable pattern as schematically shown in fig. 2a or fig. 2 b. For example, the pattern may be formed such that there is a duct 31 where nozzles are attached at a certain pitch. The term fluidization stage means fluidization stages arranged within a certain vertical distance from each other. In other words, one fluidization stage comprises nozzles 32 for introducing the reactive fluidization agent substantially at one vertical level. In other words, a reactive fluidizing agent will be introduced through the nozzle 32 in order to fluidize the solid particles and participate in the reaction. The vertical distance between the fluidization stages or stages may be evenly distributed, which means a constant distance in the vertical direction from each other. It thus ensures a proper fluidization velocity and dispersion of the solid particles in the reaction chamber from bottom to top. The size and/or shape of the nozzles 32 may be varied in one and/or more fluidization stages to provide advantageous fluidization and reaction.

The conduit 31 forms a manifold for steam or some other suitable reactive fluidising agent or fluidising agent such as air or oxygen. The cross section of the duct 31 may have a circular cross section or a rectangular cross section, just to name a few preferred cross sections. In fig. 1, the heat exchangers are arranged in a basic configuration, one layer of heat exchangers 4 being arranged per fluidization stage 3. However, changes may be made such that the number of heat exchangers 4 is greater than the number of fluidization stages 3, or the number of heat exchangers 4 is less than the number of fluidization 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 medium (water, steam, some other fluid) to transfer heat from the reactor 1. The heat exchanger inlets 41 and outlets 42 may be grouped in a suitable manner, in embodiments they may be connected in series or in parallel, and the source of the fluid of the heat exchanger may be from any suitable source. The target of the heated fluid from the heat exchanger may also be any suitable. The actual configuration of the heat exchanger depends on the reactor or plant design, the inner wall may be formed by the heat exchanger, or the heat exchanger may be configured to extend into the reaction chamber 10 (as shown in fig. 2 a) in a radial direction, and the heat transfer into the heat exchanger 4 may be based on convection or conduction, for example. The heat exchanger may comprise tubes and may be configured to extend into the reaction chamber as a tube bundle (not shown in the figures). Since the reaction and heat recovery can be uniformly performed in the reactor, the temperature of the particles to be discharged is reduced. This means that heat is recovered by the heat exchanger 4.

In fig. 2a and 2b, which represent horizontal cross-sections of the reaction chamber of fig. 1, some possible configurations of nozzles 32 arranged on the pipe 31 forming the fluidization stage 3 are schematically shown. The reactive fluidizing agent is introduced into the reaction chamber 10 through a nozzle. Non-reactive fluidizing agents may also be introduced into the reaction chamber 10 through nozzles. Because all of the drawings of the present disclosure are schematic, the elements are not shown to scale, and the relative dimensions are for illustration purposes only. However, all fluidization stages 3 are arranged in one compartment to enable efficient flow and reaction of CaO/Ca (OH) ₂ in the reaction chamber 10. Thus, the duct 31 shown in fig. 2a and 2b does not form a compartment for each fluidization stage 3, but the material may be arranged through the duct 31. Thus, clogging of particles can be avoided or reduced and operational availability and efficiency are improved compared to known solutions. With the current configuration of the fluidization stage (or in other words the fluidization-introduction stage), the reaction takes place uniformly in the reaction chamber.

In fig. 3, an embodiment of the reactor 1 is still presented, wherein the fluidization stage 3 is arranged such that in the central region of the reaction chamber 10 there is a central duct 31 serving as a manifold for the nozzles 32, and then there are nozzles arranged on the wall of the reaction chamber 10. The fluidization effect is determined by the proper orientation of the nozzle 32 and the velocity of the fluidizing medium (steam, etc.). According to the embodiment of fig. 1, 2a, 2b (as shown in cross-section) and 3, the reactor 1 is circular in cross-section perpendicular to the general flow direction and has a length that is greater than the width. This feature has an effect on the reaction time in the reactor, with the length, diameter and number of stages being properly selected as parameters for designing the reactor. Other possible reactor cross-sectional shapes are rectangular and polygonal such as hexagonal or octagonal. The heat exchanger is not shown in fig. 2b and 3, but may be arranged between the fluidization stages as in fig. 1. Similarly, as in fig. 1, one fluidization stage 3 is defined by the vertical distance of the nozzles 32 at different vertical heights.

In fig. 4, a system 100 for continuously storing and releasing thermal chemical heat energy based on one of the following reactions by utilizing one of the following reactions is schematically presented:

The system comprises a reactor 1 and wherein the system 100 further comprises a reservoir 6 for raw material and a reservoir 7 for final material, and a regeneration reactor 8 for the process of returning the final material to the raw material, the system 100 being adapted to release heat when needed and to store heat when available. Such storing and releasing energy or filling/discharging energy may be done in one location, or filling may be done where energy is available, and then transporting the filled material to a location where energy is discharged from the material in the reactor of the present disclosure.

In operation of the system 100, either 1) solid particles of alkaline earth metal in elemental form or of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn), or 2) solid particles of alkaline earth metal in oxidized form or of one of the metals from the group consisting of lithium (Li), boron (B), magnesium (Mg), aluminum (Al), silicon (Si), iron (Fe) and zinc (Zn) will be considered as raw materials storable in the reservoir 6, and the reacted compounds or in other words the end products (i.e. 1) oxidized or 2) hydrated (hydroxide) particles) are reaction materials, considered as final materials storable in the reservoir 7.

In fig. 5, an embodiment of a fluidized bed reactor (1) for continuously generating thermochemical heat energy by utilizing one of the following reactions is still presented:

The reactor 1 comprises:

the reaction chamber (10) is provided with a chamber,

At the opposite end to the first end of the reaction chamber 10, an outlet 5 is arranged for discharging the reaction material. In this example, solid particles are used as a feedstock for the process, first stored in a reservoir 6, fed through an inlet 2 to the reactor 1 and reaction chamber 10, and then fluidized, and the reaction is initiated and proceeds. In this embodiment, two rows of fluidizing nozzles are provided. The reactor may be provided with a single nozzle 32, 32a for introducing a mixture of reactive and non-reactive fluidising agents into the reaction chamber via the same nozzle 32. In the embodiment of fig. 5, the reactor is provided with two rows of nozzles 32, 32a, i.e. configured with separate nozzles, thereby providing nozzles 32 for reactive fluidizers and nozzles 32a for non-reactive fluidizers. This embodiment may be particularly suitable for materials requiring greater effort in fluidization, i.e. denser solid particulate materials or such materials. If both reactive and non-reactive fluidizers are fed into the reaction chamber 10, the material (volume) input/output balance may be such that a separate gas outlet channel 9 may be required. Depending on the actual process conditions, the gas outlet channel may be provided with a particle separator or the like to avoid solid particles escaping from the reaction chamber through this route. Such gas outlet channels may also be required for a reactor 1 having only a single type of fluidising agent feed inlet (i.e. nozzle 32 for the reactive fluidising agent) in case the process requires that the amount of reactive fluidising agent exceeds the actual amount involved in the reaction.

According to an embodiment of the method, steam is introduced as reactive fluidizer, the temperature of which gradually increases, gradually decreases or remains unchanged from the fluidization stage 3 to the subsequent fluidization stage 3. There are many modes of operation that the method and reactor and system can exist.

According to an embodiment of the present method, the steam velocity at the steam nozzle 32 gradually decreases or increases from the fluidization stage 3 to the subsequent fluidization stage 3.

While the invention has been described herein by way of examples in connection with what is presently considered to be the most preferred embodiment, it is to be understood that the invention is not limited to the disclosed embodiment, but is intended to cover various combinations or modifications of its features and several other applications included within the scope of the invention as defined in the appended claims. When such a combination is technically feasible, the details mentioned in connection with any of the embodiments above may be used in connection with another embodiment.

Parts list

1. Reactor for producing a catalyst

10. Reaction chamber

11. Inner wall

100. System and method for controlling a system

2. An inlet

3. Fluidization stage

31. Pipeline

32,32A nozzle

4. Heat exchanger

41. Heat exchanger inlet

42. Heat exchanger outlet

5. An outlet

6. Accumulator (for raw materials)

7. Reservoir (for end product)

8. Regeneration reactor

9. Gas outlet channel

Claims

1. A fluidized bed reactor (1) for continuously generating thermochemical thermal energy by utilizing one of the following reactions:

The reactor (1) comprises:

-a reaction chamber (10),

An inlet (2) arranged at a first end of the reaction chamber (10) for feeding the solid particles into the reactor (1),

An array of fluidization stages (3) is arranged inside the reaction chamber (10), wherein each of the fluidization stages (3) comprises a plurality of nozzles (32) for fluidizing the solid particles with a reactive fluidizing agent, the oxidizing agent or the hydration compound for initiating and carrying out the reaction,

The fluidization stage (3) is 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 of the first end of the reaction chamber (10) for discharging the reaction material.

2. A fluidized bed reactor (1) for continuously generating thermochemical heat energy by utilizing solid particles from the reaction of calcium oxide (CaO) +water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂),

The reactor (1) comprises:

-a reaction chamber (10),

An inlet (2) arranged to the first end of the reaction chamber (10) for feeding the solid particles of CaO into the reactor (1),

An array of fluidization stages (3) is arranged inside the reaction chamber (10), wherein each of the fluidization stages (3) comprises a plurality of steam nozzles (32) for fluidizing CaO with steam to initiate and carry out the reaction,

The fluidization stage (3) is 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 of the first end of the reaction chamber (10) for discharging Ca (OH) ₂.

3. Reactor according to claim 1 or 2, characterized in that the fluidization stage (3) is arranged in a compartment to enable solid particles such as CaO/Ca (OH) ₂ to flow in the reaction chamber (10).

4. The reactor according to any of the preceding claims, characterized in that the reactor (1) is vertical with an inlet (2) and an outlet (5) arranged in a vertical position relative to each other in the reaction chamber (10).

5. The reactor according to any one of the preceding claims, wherein the one or more heat exchangers (4) are configured to form an inner wall (11) of the reaction chamber.

6. A reactor according to any of the preceding claims, characterized in that the reactor is provided with nozzles (32, 32 a) for introducing a mixture of reactive and non-reactive fluidizing agent into the reaction chamber via the same nozzle (32), or that the reactor is provided with separate nozzles (32, 32 a) for reactive and non-reactive fluidizing agent.

7. Reactor according to any one of the preceding claims, characterized in that the reactor (1) is circular in cross-section and has a length greater than a width.

8. A reactor according to any of the preceding claims, characterized in that the reactor (1) comprises 2 to 5 fluidization stages (3), preferably 3 to 4 fluidization stages (3), in the reaction chamber (10).

9. The reactor according to any of the preceding claims, characterized in that the reactor (1) comprises a first set of nozzles (32) for fluidizing solid particles with a reactive fluidizing agent to initiate and carry out the reaction, and a second set of nozzles (32 a) for fluidizing solid particles with an inert or less reactive fluidizing agent to enhance fluidization of the solid particles.

10. A reactor according to any of the preceding claims, characterized in that the reactor is provided with a gas outlet channel (9) for discharging excess fluidization agent.

11. A method for continuously generating thermochemical thermal energy by utilizing one of the following reactions:

The method comprises the following steps:

feeding a feedstock of solid particles into a reaction chamber (10) at a first end of said reaction chamber (10),

Fluidizing the solid particles with a fluidizing jet of a first fluidization stage (3) to initiate the reaction,

Transferring the generated heat to a heat exchanger 4 in the reaction chamber (10),

Continuing the feed of raw material from the first end of the reaction chamber (10) forcing the mixture of raw material/partially reacted material to move to a subsequent fluidization stage (3) where fluidization of the mixture with fluidization jets continues and the released heat is transferred through the heat exchanger (4) at this fluidization stage (3), the mixture composition becomes more final material as the fluidization continues and after the last fluidization stage (3) the mixture contains only a small proportion of the raw material, the yield of the reaction being controlled by the fluidization stream temperature, saturation and flow rate in each of the fluidization stages,

-Removing the reaction material from the reaction chamber via an outlet (5).

12. A method for continuously generating thermochemical thermal energy from the reaction of calcium oxide (CaO) + water in the gas phase (steam) (H ₂ O) - > calcium hydroxide (Ca (OH) ₂), the method comprising the steps of:

Feeding solid particles of CaO into the reaction chamber (10) at a first end of the reaction chamber (10),

Fluidizing CaO with a steam jet of a first fluidization stage (3) to initiate the reaction,

A heat exchanger (4) for transferring the generated heat to the reaction chamber (10),

Continuing the feed of CaO raw material from the first end of the reaction chamber (10) forcing the partially reacted CaO/Ca (OH) ₂ mixture to move to a subsequent fluidization stage (3) where fluidization of the mixture with steam jets continues and the released heat is transferred by the heat exchanger (4) at this fluidization stage (3), as the fluidization continues, the CaO/Ca (OH) ₂ mixture composition becomes more Ca (OH) ₂ and after the last fluidization stage (3) the mixture contains Ca (OH) ₂ with only a small proportion of CaO, the yield of the reaction being controlled by the steam temperature, saturation and flow rate in each of the fluidization stages (3),

-Removing the reaction product Ca (OH) ₂ from the reaction chamber (10) via outlet (5).

13. A method according to claim 8 or 9, introducing steam as reactive fluidising agent, the temperature of which steam gradually increases, gradually decreases or remains unchanged from the fluidisation stage (3) to the subsequent fluidisation stage (3).

14. The method according to any of the preceding claims 8, 9 or 10, the steam velocity at the steam nozzle (32) gradually decreasing or increasing from the fluidization stage (3) to the subsequent fluidization stage (3).

15. The method of claim 7, the mixture of reactive and non-reactive fluidizers is introduced into the chamber via a nozzle, or via the same nozzle as the reactive fluidizers, or the reactor is provided with separate nozzles for reactive fluidizers and non-reactive fluidizers.

16. A system (100) for continuously storing and releasing thermal chemical heat energy based on one of the following reactions by utilizing one of the following reactions:

1) Solid particles of alkaline earth metal or metal in elemental form + oxidizing agent in gaseous or vapor form, such as steam, air or oxygen, or

2) Solid particles of alkaline earth metal or metals in oxidized form + hydrated compounds in gaseous or vapor form to obtain hydroxides,

The system comprises a reactor 1 according to any one of claims 1 to 10 for utilizing the method according to any one of claims 11 to 15, and wherein the system (100) further comprises a reservoir (6) for raw material and a reservoir (7) for final material, and a regeneration reactor (8) for the process of returning the final material to raw material, the system (100) being for releasing heat when needed and storing heat when available.