DE102007003744A1 - Reactor, for the production of nano particles, has a pulsed hot gas stream fed into the reaction zone with an adjustable frequency - Google Patents

Abstract

The thermal reactor (1), for the production of nano particles, has at least one reaction zone (2) where a hot gas stream (HGS) flows through periodically from an inlet (3). The raw material (RG) is fed in for particles to be produced, taken out through an outlet (6) with the gas to be separated by a filter. The frequency of the gas flow pulses is controlled by a valve (4). The gas is burned in a combustion zone (8) in front of the inlet, using an energy carrier (ET).

Description

The Invention relates to a method and a thermal reactor, in particular a thermal reactor for producing finely divided Particle. Such particles typically have average grain sizes from 10 nm to 100 μm, so also close nanoscale particles (also called nanoparticles) with particle sizes less than 100 nm.

in the Further, finely divided particles become a particle size of <100 μm Understood. By definition, this is the special Area of so-called nanoparticles (particle size <100 nm) included. Furthermore, powders with a mean particle diameter <100 microns referred to as finely divided powder.

to Production of finely divided powders have essentially the following manufacturing procedures have been established; chemical production in solutions (eg sol-gel method), production in plasma, Production from the gas phase (aerosol process). Depending on the application The finely divided powder is usually a well-defined and narrow Particle size distribution finely required. Depending on the chemical nature of the desired Powder is one way or another better to use to achieve good results.

to Production of finely divided oxide or mixed oxide powder has become the Pulsationsreaktor process due to process engineering peculiarities proved to be particularly suitable. The pulsation reactor differentiates In principle, other procedures in that a pulsating hot gas flow is generated. In this hot gas stream is the raw material mixture introduced, this by the thermoshock-like Decomposition reaction is converted in a few milliseconds.

One significantly increased heat transfer results due to the high flow turbulence caused by the pulsating combustion. This increased heat transfer is decisive for the course of the phase reaction in the material and for a complete turnover within a short time Residence time is.

The operating principle of the pulsation reactor is similar to that of an acoustic cavity resonator, which consists of a combustion chamber, a resonance tube, which has a relation to the combustion chamber significantly reduced flow cross-section. From the WO 02/072471 or from the DE 10 2004 044 266 A1 pulsation reactors are known. In the case of the pulsation reactors described there, the combustion space on the input side is equipped with one or more aeroventiles for the entry of fuel gas mixtures. The fuel and the necessary combustion air arrive together (premixed in an upstream mixing chamber) via the valves in the combustion chamber and are ignited there, burn very quickly and generate a pressure wave in the direction of the resonance tube, since the gas inlet is largely closed by the aerodynamic valves at overpressure , As a result of the hot gas flowing out as a result of combustion in the resonance pipe, the overpressure in the combustion chamber is reduced so that new fuel gas mixture flows in through the valves and ignites itself. This process of closing and opening the valves by pressure and vacuum is self-regulating periodically. The pulsating combustion process in the combustion chamber releases energy with the propagation of a pressure wave in the resonance tube and stimulates an acoustic oscillation there. Such pulsating flows are characterized by a high degree of turbulence. The high flow turbulences prevent the formation of a temperature envelope around the particles forming from the mixture of raw materials, whereby a higher heat transfer, ie a faster reaction at comparatively low temperatures, is possible. The consequent short residence times of the particles in the reactor lead to a particularly high material throughput. Typically, the residence time is less than one second. In addition, a particularly large proportion of the particles formed reaches a desired spherical shape. The rapid reaction also results in the formation of the solid phase of the particles to a high proportion of lattice defects and consequently to a high reactivity of the particles. For the separation of reaction products from the hot gas stream is a suitable separator for Feinstpartikel.

When Raw material components for the production of particles come different inorganic and / or organic substances into consideration. The raw material mixture can be in solid form or in the form of a Raw material solution, raw material dispersion or raw material suspension the reactor, for example by fine atomization, fed become. Particularly finely divided particles are used in the pulsation reactor process For example, if a raw material mixture consists of organometallic compounds and organic solvents is used. Especially spherical particles are obtained if an emulsion or dispersion of the raw material mixture and at least one phase immiscible therewith and produced in the pulsation reactor is abandoned.

The disadvantage of the existing pulsation reactor technology is that the throughput of high-calorie raw material mixtures is limited. High-calorie mixtures of raw materials are understood here to mean mixtures of raw materials which contain a lower calorific value of more than 4 MJ / kg. Petroleum be For example, it has a calorific value of approx. 43 MJ / kg. The (lower) calorific value is the maximum amount of heat that can be used during combustion, which does not result in condensation of the water vapor contained in the exhaust gas, based on the amount of fuel used. When using such high-calorie raw material mixtures, the combustion process in the reactor releases the calorific energy. This leads to an increase in the process temperature of the hot gas stream.

By the reduction of the fuel application (fuel gas) can this temperature increase partially counteracted. However, since the pulsating hot gas flow due to the pulsating combustion based on the design of the combustion chamber is generated with aerodynamic valves leads a reduction of the fuel quantity first to one reduced amplitude of the pulsating hot gas flow. Associated with this is the reduction in the degree of turbulence of the hot gas stream, which, however, just the desired special feature of Pulsationsreaktor - method represents. When falling below a necessary amount of fuel Ultimately, the pulsating hot gas production breaks down together.

The desired process temperature (treatment temperature) results in the pulsation reactor according to the generation of the pulsating Hot gas flow (amount of fuel) and the caloric heat content the raw material mixture. From this context arise typical Feed quantity from the technical operation of the pulsation reactor for an aqueous salt solution as a raw material solution of about 60 kg / h and a mixture of raw materials consisting of organometallic Compounds in organic solvents or for the use of raw material emulsions of approx. 15 kg / h. A lower one Feed quantity (throughput) increases the specific production costs.

One Another known disadvantage of Pulsationsreaktor technology is that the frequency of the pulsating hot gas flow can not be directly influenced or adjusted. The main influencing factors on the frequency of the pulsating hot gas flow are the geometry of the reactor (Helmholtz resonator), type and quantity the raw material mixture as well as the process temperature. The geometry of the reactor is stationary. Indirectly, the frequency can be adjusted accordingly the process temperature can be varied, these being in the technical Operation by the necessary treatment temperature substantially is predetermined. De facto, the frequency of the pulsating hot gas flow currently not be discontinued. However, since just this vibrant Hot gas flow the particular reaction conditions in the reactor generates, reduces the non-variable frequency of the pulsating Hot gas flow the power of the Reactor.

Of the The invention is therefore based on the object, an improved method and a thermal reactor for producing fine particles in which a mixture of raw materials in a pulsating hot gas flow is treated in the pulsating hot gas stream from the Raw material mixture forming the finely divided particles, the frequency the pulsating hot gas flow is adjustable.

The The object is achieved by a thermal reactor having the features of claim 1 and a method having the features of claim 15.

advantageous Embodiments of the invention are the subject of the dependent claims.

A thermal reactor according to the invention for the production of particles comprises at least one reaction space, wherein one of the reaction spaces is periodically fed with a hot gas stream through a hot gas inlet. Together with the hot gas flow through the hot gas inlet or separately through a feed point, a raw material mixture which comprises at least one raw material component can be supplied to this reaction space. From at least one of the raw material components particles are formed in the hot gas stream and discharged through an outlet from this reaction space or fed to another of the reaction spaces. By at least one controllable first valve at the hot gas inlet or upstream of this and / or by a periodic combustion of at least one hot gas stream forming energy carrier and / or at least one of the energy carrier used, the hot gas stream forming raw material components with controllable combustion frequency in at least one of the hot gas inlet upstream combustion chamber is a Frequency of the periodic supply of the hot gas stream predetermined. An optionally existing connection between the combustion chamber and the reaction space should be considered as part of the reaction space. Such a designed thermal reactor, which is operated by the method described, combines the known from the prior art benefits of particle formation in a pulsating hot gas flow with the possi probability, a frequency of the pulsating hot gas flow regardless of the geometry of the reaction chamber and the caloric content of the Pretend raw material mixture. The predetermined periodic supply of the hot gas stream into the reaction chamber also makes it possible to use high-calorie raw material mixtures without the need to throttle the fuel supply such that the pulsation of the hot gas stream is significantly influenced or collapses in its amplitude. The particle formation can already start in the combustion chamber.

Of the Combustion chamber is a reaction space in which the energy source introduced periodically or continuously and for ignition is brought. This forms the hot gas stream, the gaseous components, but also solid and / or liquid components.

The formed particles are preferably in a filter, the one the reaction chambers downstream, deposited.

When Energy sources are substances with high caloric content be understood that in a thermal reaction, a heat of reaction deliver. These include, for example, typical solid, liquid or gaseous fuels. The released heat energy generates the treatment temperature in the hot gas.

In a preferred embodiment provides at least one the raw material components at least partially the energy source for the process is therefore a high calorific raw material component z. B. in the form of a solid, a liquid or a gas. At first, all of them are responsible for the formation of the particles necessary raw material components contained in the raw material mixture. additionally can the raw material mixture auxiliary components as raw material components contain, for example, solvents, in particular organic Solvents. An example of such a high calorie Commodity Blend is the combination of organometallic compounds and organic solvents, another example Commodity Blend in the Form of Raw Material Dispersions or Emulsions as auxiliary component a Dispergens contain, as high caloric organic component can be formed.

The Production of a raw material dispersion, raw material suspension or raw material emulsion is a way to adjust the particle size. A dispersion should be a mixture of at least two substances be understood that are not or hardly miscible with each other. One of the substances (disperse phase) is possible finely dispersed in another of the substances (dispersant). A suspension is a dispersion in which the disperse phase is a solid and the dispersant is a liquid. Under an emulsion is a finely divided mixture of two different (usually immiscible liquids) without visible Understood demixing. The so-called inner phase (disperse phase) lies in small droplets distributed in the so-called outer Phase (continuous phase, dispersant, dispersant) before. emulsions belong thus to the disperse systems, are thus one Special case of a dispersion. Another ingredient of all emulsions is an emulsifier that lowers the energy of the phase boundary and so on Counteracts segregation. To stabilize immiscible liquids For example, surfactants such as emulsifiers, Surfactants, to be added. They prevent the mixture again separates into its components. Other special cases of dispersions are gels, aerosols, foams and colloids. Disperse systems can also appear nested. So For example, the disperse phase of a dispersion itself Be dispersion.

Of the Use of raw material dispersions or raw material emulsions leads to finely divided powders with particularly spherical particles and a particularly narrow particle size distribution. The expert can easily from the rich offer on excipients for the preparation of dispersions or emulsions specific groups or individual representatives for each Select the application and through routine tests the Optimize application for each requirement.

Lies the caloric energy of the raw materials batch under the necessary Heat content to reach the desired process temperature in the reaction space, can the raw material batch before or during the task in the combustion chamber through at least one combustion chamber inlet opening an additional energy source in the form of a gas or a liquid. Suitable as fuel gas basically any gas that is used for hot gas production suitable is. Preferably, natural gas and / or hydrogen is used. Alternatively, propane or butane or mixtures of different Fuels are used as energy sources. The mixture the raw material mixture and the additional energy source For example, in one of the combustion chamber inlet opening upstream mixing chamber done.

Of the Energy carrier (high caloric component) is preferred periodically in the combustion chamber. There the ignition of the Energy carrier. The ignition can be solely due to the prevailing in the combustion chamber high temperatures, if necessary in combination with high pressures (comparable to engines) by auto-ignition and / or by an additional Ignition source done. The ignition source can burn continuously (pilot flame, pilot burner, Supporting flame) or switched on periodically. Next a continuous pilot flame, for example into consideration: glow plugs, spark plugs, electric heated glow wires or glow grids.

In a preferred embodiment, the energy carrier to the combustion chamber via a Nozzle trained Brennraumeinlassöffuung supplied. The type of nozzle depends on the specific conditions of the raw material batch and on the desired process parameters. Due to the nature of the nozzle, the droplet size, the droplet size distribution and the distribution of the droplets in the combustion chamber or reaction space can be adjusted. For example, one- and two-fluid nozzles, perforated nozzles, multi-hole injection nozzles, and pin nozzles can be used. The advantage of using a nozzle is the task of finely distributed droplets which ensure a fast reaction conversion due to their high surface area.

Of the pressure applied to the nozzle is the same as the design of the nozzle itself, a significant factor on the droplet size, the droplet size distribution and the distribution of the droplets in the combustion chamber or reaction space. At higher pressures, for example, in principle reached smaller drop sizes. The pressure is generated by a pump or a pump system and is preferably variably adjustable.

Of the Combustion chamber is typically formed as a closed vessel, which at least one combustion chamber inlet opening for the energy carrier and / or for the raw material mixture and / or for at least one further gaseous Component (eg reaction gases). On the output side points the combustion chamber an opening for the outflow of the hot gas mixture containing the hot gas inlet of the reaction space forms or leads to this.

Of the Combustion chamber preferably has flow elements which for additional turbulence of the reaction components in the combustion chamber and finally to more homogeneous reaction conditions amount to the combustion chamber cross section.

The The shape of the combustion chamber influences the combustion process and thus the resulting properties of the particles. For one low variation in particle quality the combustion chamber are designed such that almost the same reaction conditions present at any point in the interior. Here is the vote the combustion chamber geometry with the nozzle used as well further applied reaction parameters (for example nozzle pressure) required.

The Output side opening of the combustion chamber to escape the hot gas stream, d. H. the hot gas inlet of the Reaction space, can be unlocked, but also periodically closed be, for example by a controllable first valve.

In a preferred embodiment, the combustion chamber a cylindrical space. The combustion chamber inlet opening or the combustion chamber inlet openings, for example solenoid valves, is or are periodically opened and closed. On the output side allows a conical opening the hot gas outlet, this is not lockable.

In Another preferred embodiment is the combustion chamber the combustion chamber of a cylinder of a conventional internal combustion engine, for example, a reciprocating engine or a rotary piston engine. He points next to the input side combustion chamber inlet openings for energy sources and / or raw material mix and / or additional gaseous components (for example formed as a second valve) on a movable piston. The hot gas outlet occurs periodically, also via a hot gas inlet the first reaction chamber acting first valve. The way of working Such an engine is typically cyclic in a reciprocating engine for example, in several, z. B. two or usually four bars. It Several of these combustion chambers can take the form of several Cylinder of the internal combustion engine to be arranged in parallel, whose Hot gases, if necessary, each have their own first valve exhausted, in a kind of exhaust manifold brought together and fed to the reaction space. The distance from the first valves via the exhaust manifold up to the reaction space can be considered as a hot gas inlet become.

The following is a typical sequence of operations in a cylinder of such an internal combustion engine is shown, which also takes place in the combustion chamber of the thermal reactor in this preferred embodiment. There are a number of different internal combustion engines, which are in principle also suitable for the process for the preparation of the particles. At the first cycle, the intake of combustion air takes place as a further gaseous component, optionally in combination with other gaseous components (process gases). For this purpose, the piston is at top dead center and begins to move downwards. The intake valve serving as the second valve opens at the combustion chamber intake port, and the combustion air is drawn into the cylinder (here, the combustion chamber). When the piston reaches bottom dead center, the second valve is closed. At the 2nd stroke, the gas or gas mixture in the cylinder (here combustion chamber) is compressed by the upward movement of the piston. If the piston has reached near top dead center, the energy carrier is injected with the raw material mixture, for example through a combustion chamber inlet opening formed as a nozzle. The energy source ignites, possibly with the help of a spark plug. At the 3rd clock, the expansion of the hot gas produced by the combustion and thus the downward movement of the piston take place. In the 4th cycle, the outlet valve serving as the first valve is first opened, and the hot gas flows through a renewed upward movement of the piston out. The exhaust valve closes shortly after the piston reaches top dead center. In a combustion chamber designed in this way, it is possible to produce particularly finely divided particles, since particularly fine droplets are formed by the high pressure in the combustion chamber, from which the finely divided particles are subsequently formed. It was found that the targeted production of finely divided powders with a very homogeneous product quality is technologically possible if the combustion chamber inlet opening (second valve), the combustion chamber and the piston are adapted to the extremely high proportion of solids compared to gasoline or diesel.

For example, ambient air is used as combustion air; alternatively, oxygen or a mixture of both can be used. In addition, the gas atmosphere in the combustion chamber can be adjusted in a targeted manner by adding further gaseous components, for example CO ₂ , and thus offers a further control variable for setting the reaction parameters in the thermal production and treatment of the finely divided particles. The gaseous components can be supplied to the combustion chamber separately and / or together with the energy carrier and / or the raw material mixture. With common task of the raw material mixture and / or the energy carrier, their mixing can take place, for example, in an upstream mixing chamber or a mixing nozzle.

The periodic supply of the energy carrier in the Combustion chamber, the following ignition of the energy carrier, the subsequent at least partial thermal conversion of the energy carrier (combustion) with the associated Formation of the hot gas mixture (volume increase) and the subsequent Outflow of the hot gas mixture leads to a pulsating hot gas stream in the reaction space.

The Combustion frequency in the combustion chamber is preferably in a range from 3 Hz to 200 Hz, in particular 10 Hz to 100 Hz and can, for example, about the control of the periodic supply of the energy carrier be varied. In this frequency range, the process engineering Parameter controlled particularly stable for a long time and thus ensure consistent product quality become.

Of the pulsating hot gas flow is from the combustion chamber through the Hot gas inlet into at least one of the combustion chamber introduced subsequent reaction space. Under a reaction room should In this case, each structure can be understood, which is at least one Residence time of the hot gas flow generated in the combustion chamber of generation until the filter is extended. The design the reaction space depends on the type of thermal desired Treatment of the raw material mixture or the resulting finely divided Powder off. In this case, a coupling of several different reaction spaces be advantageous for a stage thermal treatment. Due to the selected geometry in connection with The selected process control can be one of the reaction chambers also as a drying room, as a calcination room and / or as a phase conversion room space to be used.

In a preferred embodiment is the connected Reaction space a tube-like structure, with outlet and / or hot gas inlet are made conical can. The diameter and the tube length determine while essentially the residence time of the hot gas stream in this reaction space and can according to the necessary reaction conditions are adjusted.

• – periodisch (pulsierend) in den Brennraum, dabei kann eine Rohstoffkomponente selbst als wesentlicher Energieträger dienen, gegebenenfalls gemeinsam mit einem oder mehreren zusätzlichen Energieträgern, wie beispielsweise Erdgas, Diesel, Petroleumbenzin etc. oder
• – kontinuierlich in den Brennraum und/oder den angeschlossenen Reaktionsraum, zum Beispiel durch feines Einsprühen, dabei wird mindestens ein Energieträger, wie beispielsweise Erdgas, Diesel, Petroleumbenzin etc., periodisch dem Brennraum zur Erzeugung der pulsierenden Verbrennung zugeführt.

The supply of the raw material mixture in the thermal reactor is either

• - Periodic (pulsating) in the combustion chamber, while a raw material component itself serve as an essential energy source, optionally together with one or more additional energy sources, such as natural gas, diesel, petroleum spirit, etc. or
• - Continuously into the combustion chamber and / or the connected reaction space, for example by fine spraying, while at least one energy source, such as natural gas, diesel, petroleum spirit, etc., periodically fed to the combustion chamber to produce the pulsating combustion.

to Supply of the raw material mixture at different positions of the thermal reactor (combustion chamber, reaction chamber) has this different feed points. The choice of the feed point significantly influences the thermal treatment of the raw material mixture or the resulting finely divided particles and thus the properties the finely divided powder. This is the choice of the feed point a relevant tax code for the product properties

The raw material mixture can be introduced in the form of solid raw materials, as a raw material solution, raw material suspension, raw material dispersion or raw material emulsion, for example sprayed or atomized. In addition, the raw materials or raw material mixtures can be introduced in gaseous form in the thermal reactor. For this purpose, the raw materials or the raw material mixture are first transferred outside the described thermal reactor in the gas phase, z. B. fed by an evaporator and the thermal reactor. There is also the possibility of combining ver various forms of delivery.

in the Case of a solid or gel as raw material or raw material mixture The material is preferably via a downpipe from above fed into the reaction space. For example, the Solid and / or the gel against the flow sense of the hot gas stream given up. Due to the length of the downpipe, the job site and thus the residence time of the solid can be varied.

in the Case of a raw material solution, raw material suspension, raw material dispersion or raw material emulsion as a mixture of raw materials takes place the product task preferably by means of a nozzle, for example by a two-fluid nozzle or high pressure injector. The type of nozzle influences the potty training and thus the resulting Particle shape or particle size distribution. The Injection direction with respect to the pulsating hot gas flow For example, it can influence process parameters such as residence time and degree of turbulence. Also, the spray pattern, in particular the droplet size distribution affected. This is the choice of the injection direction a significant control factor for the residence time, Turbulence level and particle size distribution.

In In another preferred embodiment, the injection direction in the direction of flow of the hot gas stream, for example at a feed point in the combustion chamber or in the reaction space, selected. This is the pulsating hot gas flow least affected.

In In another preferred embodiment, the raw material mix becomes through the nozzle against the flow direction of the Medium flow of the pulsating hot gas, in particular in the reaction chamber sprayed. The task can continue at any angle to the direction of flow of the hot gas stream respectively.

In Another preferred embodiment is the raw material mixture periodically abandoned in the combustion chamber of the thermal reactor. At least one of the raw material components serves as an essential energy source for the process. If necessary, the raw material mixture additional energy sources are added.

to Formation of the raw material mixture will initially be raw material components in the corresponding stoichiometric ratio combined. As raw material components for the production the particles come, for example, inorganic and / or organic Substances such as nitrates, chlorites, carbonates, bicarbonates, carboxylates, Alcoholates, acetates, oxalates, citrates, halides, sulfates, organometallic Compounds, hydroxides or combinations of these substances into consideration. These substances are the basic components of the raw material mixture. commitment can find solid and / or liquid raw material components.

to Production of raw material mixtures in the form of solutions or suspensions are optionally auxiliary components as further Raw material components needed. To form a solution becomes added a solvent as an auxiliary component, in which the example solid base component solved becomes.

It can be further auxiliary components, such as surfactants, to reduce the surface energy to liquid Mixed raw materials are added. This allows the drop size when spraying the raw material mixture in the thermal Reactor can be influenced and adjusted.

Farther may be an organic and / or inorganic caloric component be added as a raw material component or auxiliary component. In order to is meant a component that in addition in a thermal process caloric energy within the forming particle and / or releases in the area between the particles and thus for example accelerates a phase formation or by an explosive thermal conversion leads to rupture of the discontinued droplets. By the task or thermal treatment of smaller droplets Initially, particles with a smaller particle diameter are formed.

A For example, particularly narrow and defined particle size distribution of the particles by a single or multi-stage wet-chemical intermediate step be achieved before the thermal treatment in the thermal reactor. This can be done through the way and process management of the wet-chemical intermediate step, for example via a so-called co-precipitation, the particle size initially set in the raw material mix. In the Adjustment of the particle size is to be considered, that they are changed by the following thermal process can. For the wet-chemical intermediate step of an aqueous and / or alcoholic raw material mixtures may be known Methods such as co-precipitation or hydroxide precipitation be applied.

The necessary thermal treatment temperature of the raw material mixture or of the finely divided particles formed therefrom is fundamentally specific to the fine-particle powders to be produced. The thermal reactor therefore has, at least in part, a variable and modifiable temperature profile with a wide range of variation. The maximum temperature of the hot gas is preferably in the range between 200 and 2000 ° C, preferably between 400 ° C and 1500 ° C. The attitudes The temperature can be controlled and controlled, for example, via the type and quantity of the energy carrier, via process-technical parameters such as volume flow or by supplying defined quantities of cooling media (cooling gas / cooling liquid) to at least one further feed point.

Preferably is the temperature profile of the hot gas flow over the entire thermal reactor (combustion chamber, reaction chamber and in the range before and in the filter) adjustable. For this purpose, the thermal Reactor the possibility of additional task of energy carriers (secondary firing) or the abandonment of Cooling gas or coolant at different Feed points on.

In A preferred embodiment is the process temperature at the feed point of the raw material mixture by a reduced Energy input is limited and is by supplying a additional energy carrier (secondary firing) later elevated. This solves the problem that it through the thermal shock treatment of certain raw material mixtures, especially when using aqueous raw material mixtures (Nitrate solutions), to a crust formation in the sprayed Raw material droplets by evaporation on the droplet surface and the associated concentration of the ingredients the droplet surface, can come. This crust first stands the escape of formed gaseous Substances (eg thermal decomposition of the solvents or removal of nitrate) from the interior of the raw material droplets opposite. However, gas pressure eventually causes the crusts broken up and form particles with so-called hollow sphere structure. However, the formation of particles with hollow spherical structure is for certain applications undesirable. Here is a spherical Form preferred. At a reduced process temperature occurs not in any case a complete conversion. However, it succeeds by introducing an additional amount an energy source (for example natural gas or hydrogen), increase the energy input at the time when for example, no more solvent inside the particles is present (secondary firing). This energy is used, for example to thermally decompose any remaining salt and the transformation of the material, for example, phase formation, accelerating or completing.

In Another preferred embodiment is the process temperature clearly reduced in the reaction chamber connected to the combustion chamber the process temperature in the combustion chamber. This opens up the Possibility of thermal treatment of the raw material mixture or the resulting finely divided particles at process temperatures in the range of 100 ° C to 750 ° C if sufficient Residence times (depending on the geometry of the reaction space). As a result, for example, the formation of finely divided hydroxide or hydrate powders, such as Ca-phosphate hydrates. To adjustment a lower compared to the combustion chamber process temperature in the reaction space, the hot gas stream is supplied by feeding a cooling medium, in particular of cooling gas and / or Coolant cooled. The cooling can, for example, between the combustion chamber and the reaction space or take place at the beginning of the reaction space. In an advantageous way the cooling is realized such that the hot gas flow not in its basic direction of flow changed or the pulsation of the hot gas flow not completely prevented.

To The formation of the particles in the thermal reactor can be an at least Partial one- or multi-stage in-situ coating (the special case Impregnation is here under the concept of coating including) the particles in the pulsating hot gas stream respectively. For this purpose, at least one coating composition on a in the pulsating hot gas stream a place of particle formation abandoned place. It is at a suitable choice the process flow both a purely inorganic coating as also an organic coating or a combination of both possible. The flexibility in pulsating hot gas production and the design of the reaction chamber offers extensive adjustment options the process parameter and thus the possibility of different Coating forms, for example layer thickness or modification the coating, to realize. Through the process control, for example by the process temperature at the point of addition, the residence time and / or by the choice of the educts of the coating composition, the desired coating form can be realized.

advantage the in-situ coating on this thermal reactor is that the formed finely divided particles first Deagglomerated as far as possible in the pulsating hot gas stream present and thus a simple coating can be done. A Coating of the finely divided powders produced in a separate Treatment step (outside the thermal reactor) is much more difficult because the finely divided particles outside the thermal reactor or the hot gas stream alone deagglomerated due to their high specific surface area available.

The coating of the particles can serve, for example, to reduce the agglomeration tendency of the finely divided particles, make the coated particles easier to incorporate into liquids, and / or to adapt the product properties of the finely divided powders to application-specific ones Conditions are adapted. For this purpose, the coating composition can be added in gaseous and / or liquid form to the pulsating hot gas stream.

In In a preferred embodiment, the formed finely divided particles coated with organic substances. there the organic coating composition is passed through in liquid form fine spraying at a feed point in abandoned the thermal reactor at which the process temperatures is less than 300 ° C. If necessary, the temperature the pulsating hot gas flow previously by feeding a cooling medium reduced.

In Another preferred embodiment is an inorganic Coating thereby realized that the pulsating hot gas flow added a coating in gaseous form becomes. The gaseous components of the coating composition store themselves as a result of the thermal treatment on the surface of the particles formed and coat them at least partially. Such deposition of the coating components on the surface For example, the particle may be reduced by condensation in succession Temperature of the pulsating hot gas flow done.

The in the thermal reactor produced finely divided particles are with a suitable filter, such as a gas cyclone, hot gas filter Surface filter, an electrostatic filter or a bag filter, separated from the hot gas stream.

The Hot gas is applied to the filter before entering the filter cooled according to the type of filter required temperature. This is done for example by a heat exchanger and / or by introducing cooling gases into the hot gas stream.

The Particles can have an additional one-stage or multi-stage thermal aftertreatment, to at least partially modify their surface and / or any remaining volatile components (For example, carbonates, nitrates, etc.) at least partially remove. For the ther mix after treatment is preferably another thermal reactor, in particular a rotary kiln or a fluidized bed plant used.

The finely divided particles are used in a further embodiment before and / or during at least one of the thermal after-treatments at least partially coated or impregnated. It can possible agglomerations of the coated particles preferably be at least partially reduced by a dry grinding.

The finely divided particles, coated or uncoated be transferred into a suspension, wherein a Agglomeration of the particles in the suspension by an additional Wet grinding at least partially reduced and / or the suspension can be dried, for example, to a granulate.

embodiments The invention will be described in more detail below with reference to drawings explained.

In this demonstrate:

1 a schematic representation of a thermal reactor with a reaction space,

2 a schematic representation of the thermal reactor with a reaction space and a first valve,

3 a schematic representation of a thermal reactor with a combustion chamber,

4 a schematic representation of a thermal reactor with a combustion chamber, a piston and a first valve serving as an outlet valve, and

5 a schematic representation of another embodiment of a thermal reactor for longer residence times.

each other corresponding parts are in all figures with the same reference numerals Mistake.

1 shows a thermal reactor 1 for the production of particles P. The thermal reactor 1 includes a reaction space 2 , via a hot gas inlet 3 a hot gas flow HGS is supplied periodically. A frequency of this periodic supply is provided by a controllable first valve 4 at the hot gas inlet 3 or this is arranged upstream, given. The formation of particles P is the reaction space 2 fed a raw material batch RG. This includes raw material components RK. The particles P are formed from at least one of these raw material components RK. The feed of the raw material mixture RG can be combined with the hot gas flow HGS through the hot gas inlet 3 or separately through one of possibly multiple feed points 5 respectively. Both possibilities are shown. When feeding the raw material mixture RG with the hot gas flow HGS, the particle formation can already before reaching the reaction space 2 start in the hot gas stream HGS. The particles formed from the raw material batch RG or at least one of its raw material components RK are discharged through an outlet 6 from the reaction space 2 dissipated.

In addition, the reaction space can 2 about the feed points 5 additional process gases are supplied for setting a defined reaction atmosphere. About the feed points 5 It is also possible to supply cooling media KM, such as cooling water or cooling air, or further energy sources ET for the targeted adjustment of a temperature profile or coating components or coating mixtures BM for coating the finely divided particles P already formed.

It may be following the reaction space 2 further reaction rooms 2 ' be provided for further process steps before the particles P by means of a filter 7 (not shown) are separated from the hot gas stream HGS. There may be several first valves 4 be arranged in parallel so that they merge hot gas streams HGS from different sources.

2 shows an alternative embodiment of the thermal reactor 1 where the hot gas inlet 3 not through a first valve 4 is closable. The periodic supply of the hot gas stream HGS into the reaction space 2 can here by a periodic combustion of an energy source ET or used as energy source of raw material components RK with controllable combustion frequency in a reaction space 2 upstream combustion chamber 8th respectively. A combination with a first valve 4 at the hot gas inlet 3 or upstream of this is also possible. Raw material mix RG and / or energy sources ET and / or optionally other gaseous components GK, such as combustion air to the combustion chamber 8th through at least one combustion chamber inlet opening 9 supplied separately or together.

3 shows an embodiment of a thermal reactor 1 for the production of finely divided particles P having an average particle size of 10 nm to 100 μm. The geometry of the thermal reactor 1 corresponds in the example of a conventional pulsation reactor. This includes the thermal reactor 1 a combustion chamber 8th for producing a pulsating hot gas flow HGS An energy carrier ET is periodically introduced into the combustion chamber 8th via a combustion chamber inlet opening 9.3 or 9.4 given up. In the example shown, the energy carrier is one of several raw material components RK of a raw material mixture RG. As raw material components RK organic metal compounds and solvents are provided. The raw material mixture RG is by means of a in one of the combustion chamber inlet openings 9.1 to 9.n. nozzle periodically fine into the combustion chamber 8th sprayed. As energy sources ET can the combustion chamber 8th but also combustible gas, eg. As hydrogen, or liquid fuel, such as. As gasoline, are supplied.

Other gaseous components GK, such as combustion air VL and possibly other process gases are, via a further combustion chamber inlet opening 9.1 in the combustion chamber 8th abandoned, in the example shown separately from the supply of the energy source ET. However, the supply of the further gaseous components GK can also take place together with the energy carrier ET. For this purpose, a predetermined mixing chamber can serve for mixing (not shown). In the example shown, the combustion chamber 8th Ambient air as combustion air VL via the combustion chamber inlet opening 9.1 fed continuously.

The combustion chamber inlet opening 9.1 and 9.2 can do this in a bottom of the combustion chamber 8th or above the floor in the combustion chamber 8th lead. Preferably, the combustion chamber inlet opening opens 9.2 in an opening cone in the bottom of the combustion chamber 8th ,

The periodically abandoned energy source ET, in the example shown a highly calorific of several raw material components RK of a raw material mixture RG, is in the combustion chamber 8th with the participating in the combustion of the other gaseous components GK, such as the combustion air VL ignited. This is done for example via a periodically or continuously burning ignition source 10 , in the example shown via a continuously burning pilot burner (pilot flame).

The energy carrier ET and the other gaseous components GK (eg the combustion air VL) burn very rapidly and generate a pressure wave. On the output side, the combustion chamber 8th an opening, in the example shown, a non-closable opening in the form of a hole. This forms the hot gas inlet 3 of the reaction space 2 or leads to this. The generated pressure wave can propagate only in the direction of the outlet-side opening, as in the direction of the combustion chamber inlet openings 9.1 to 9.n. Measures to prevent the gas leakage are made. For example, in the combustion chamber inlet openings 9.1 to 9.n. second valves 12 be provided in the manner of inlet valves.

To the opening of the combustion chamber 8th closes the reaction space 2 at. In the example shown, the reaction space corresponds 2 a resonance tube. The resonance tube can also have a bend, for example by 90 °. By the outflow of the generated hot gas flow HGS from the combustion chamber 8th in the reaction space 2 Reduces the pressure in the combustion chamber 8th clear. The fact that the supply of the energy carrier ET and the subsequent abrupt combustion periodically expire, the process of the outflow of hot gas is repeated from the combustion chamber 8th in the reaction space 2 also periodically. The hot gas flow HGS pulsates.

In the reaction room 2 are different feed points 5.1 to 5.n intended. The feed points 5.1 to 5.n are formed for example as nozzles. In addition, the raw material batch RG, a further energy source ET for the purpose of secondary firing, a coating amount BG, auxiliaries or cooling media KM can be introduced into the hot gas stream HGS. In the example shown, the raw material batch RG is periodically already in the combustion chamber with a raw material component RK serving as an energy source ET 8th led, the feeder point 5.2 serves to introduce cooling air as cooling medium KM in order to significantly reduce the temperature of the pulsating hot gas flow HGS from this point. This serves in this case to prevent sintering effects, such as particle growth or "Sinterhalsbildung".

In the hot gas flow HGS, particle formation takes place from the raw material batch RG. The generated hot gas flow HGS preferably has a combustion frequency of 5 Hz to 200 Hz. By the choice of the feed point 5.1 to 5.n or the combustion chamber inlet openings 9.1 to 9.n. for the task of raw material mixture RG and other substances is both a reaction temperature, which follows in the course of the hot gas flow HGS a certain profile, as well as the order of the reactions for particle formation and / or coating aufeinan of the following process steps in the thermal reactor 1 influenced. The finely divided particles P formed in the hot gas stream HGS then pass into a filter 7 that attach to the reaction space 2 followed. In the filter 7 the formed particles P are separated from the hot gas flow HGS.

In a further advantageous embodiment, the thermal reactor 1 in the area of a closing cone of the combustion chamber 8th be provided in the output-side area at least with a flow element. This supports a turbulence of the pulsating hot gas flow HGS, whereby a better mixing of the raw materials or the raw material mixture RG is possible. In a particularly simple embodiment, the resonance tube (here reaction chamber 2 ) at least partially into the closing cone.

4 shows an alternative embodiment of a thermal reactor 1 for the production of finely divided particles P having an average particle size of 10 nm to 100 μm. The thermal reactor 1 has a combustion chamber 8th for generating the pulsating hot gas flow HGS. The combustion chamber 8th includes a piston 11 , which can perform mechanically reversing translational movement. Furthermore, the combustion chamber includes 8th On the input side, a combustion chamber inlet opening 9.1 in the illustrated example for supplying the combustion air VL with a second valve 12 , a combustion chamber inlet opening 9.2 for the raw material batch RG, in the example shown in the form of a nozzle and on the output side as a hot gas inlet 3 of the reaction space 2 serving combustion chamber outlet for the generated hot gas flow HGS, in the example shown with a controllable first valve 4 closable.

The in 4 illustrated combustion chamber 8th It works according to the operating principle of a four-stroke engine (in the example shown in the form of an engine with internal mixture formation, such as in diesel engine or gasoline direct injection). The piston 11 is at top dead center and starts to move down. The inlet valve (second valve 12 at the combustion chamber inlet opening 9.1 ) opens and combustion air VL is in the combustion chamber 8th sucked. When the piston 11 reaches the bottom dead center, the combustion chamber inlet opening 9.1 closed. The piston 11 now moves up and compresses the in the combustion chamber 8th combustion air VL. About the combustion chamber inlet opening 9.2 the raw material batch RG is injected with organometallic compounds and organic solvents as raw material components RK. At least one of the raw material components RK, for example the solvent, serves as an energy source ET. The energy source ET ignites in connection with the combustion air VL due to the high pressure and the high temperature. Alternatively, the mixture may also be ignited by, for example, a spark plug. The burning mixture expands and pushes the piston 11 downward. When the piston 11 reaches bottom dead center, becomes the first valve 4 open. By the upward movement of the piston 11 is the generated hot gas flow HGS from the combustion chamber 8th pushed. The first valve 4 closes shortly after the piston 11 has reached the top dead center.

The in 4 illustrated combustion chamber 8th with the principle of operation of an engine with internal mixture formation is a preferred embodiment and may alternatively by other embodiments, for example by operating principles comparable to engines with external mixture formation, for. As gasoline gasoline engine or indirect gasoline injection, be replaced.

Through the first valve 4 the generated hot gas flow HGS leaves the combustion chamber 8th and passes over the hot gas inlet 3 in the connected reaction space 2 , here in the form of a resonance tube. Alternatively, the reaction space 2 have other geometric shapes depending on the desired thermal treatment profile of the raw material mixture RG or the thereof to be formed finely divided particles P. The generated hot gas flow HGS pulses due to the periodically proceeding combustion process.

In the reaction room 2 There are different feed points 5.1 to 5.n , The feed points 5.1 to 5.n are formed for example as nozzles. In addition, the raw material batch RG, another energy source ET, coating mixed BG, auxiliaries or cooling media KM can be introduced into the hot gas flow HGS. In the example shown, the raw material batch RG with the raw material component RK serving as energy carrier ET is periodically already in the combustion chamber 8th over the combustion chamber inlet opening 9.2 supplied, the feed point 5.4 serves to introduce cooling air as cooling medium KM in order to significantly reduce the temperature of the pulsating hot gas flow HGS from this point. This serves in this case to prevent sintering effects, such as particle growth or "Sinterhalsbildung".

In the hot gas flow HGS, particle formation takes place from the raw material batch RG. The generated hot gas flow HGS preferably has a combustion frequency of 5 Hz to 200 Hz. By the choice of the feed point 5.1 to 5.n is both a reaction temperature, which follows a certain profile in the course of the hot gas flow HGS, as well as the order of the reactions for particle formation and / or coating in successive process steps in the thermal reactor 1 influenced. The finely divided particles P formed in the hot gas stream HGS then pass into the filter 7 that attach to the reaction space 2 followed. In the filter 7 the powder deposition takes place by separating the particles P formed from the hot gas stream HGS.

5 shows a further embodiment for a thermal reactor 1 for the production of finely divided particles P having an average particle size of 10 nm to 100 μm. This includes the thermal reactor 1 a combustion chamber 8th for generating the pulsating hot gas flow HGS analogous to in 3 shown combustion chamber 8th ,

To the outlet-side opening of the combustion chamber 8th closes a reaction space 2 at that other than in 3 is formed. The reaction space 2 has the shape of a cylindrical vessel, the hot gas inlet 3 ie the connection between the combustion chamber 8th and reaction space 2 conical in the reaction space 2 enters.

In the example shown, the combustion chamber 8th an energy source ET in the form of conventional diesel fuel via the combustion chamber inlet opening 9.2 supplied periodically. About the combustion chamber inlet opening 9.1 the supply of combustion air VL takes place in the form of ambient air.

About the feed point 5.1 the introduction of cooling air as cooling medium KM takes place in the hot gas inlet 3 that is part of the reaction space 2 should be considered. As a result, the temperature of the pulsating hot gas flow HGS, which from the combustion chamber 8th emanates, reduced. This allows the process temperature in the reaction chamber 2 be set between 200 ° C to 800 ° C. This is advantageous, for example, if the finely divided particles produced are to have P phases which are stable at these temperatures and can therefore be formed.

The raw material batch RG is in the example shown on the feed point 5.2 the reaction space 2 and thus the pulsating hot gas flow HGS by fine atomization by means of a feed point 5.2 arranged two-fluid nozzle supplied. The finely divided particles P are formed in the subsequent time in the pulsating hot gas flow HGS 3 enlarged reaction space 2 is the prolonged residence time of the hot gas stream HGS and thus of the raw material mixture RG or the resulting finely divided particles P.

The finely divided particles P formed in the hot gas stream HGS then pass into a filter 7 that attach to the reaction space 2 followed. In the filter 7 the powder deposition takes place by separating the particles P formed from the hot gas stream HGS.

The The following examples illustrate the present invention. However, they are by no means to be considered limiting. All Compounds or components used in the preparations can be either known or for sale available or can by known methods be synthesized. The temperatures given in the examples always valid in ° C. It goes without saying that both in the description and in the examples the added amounts of the components in the compositions always add up to a total of 100%. Given percentages are always to be seen in the given context. They usually relate but always on the mass of the stated partial or total quantity.

Example 1)

The raw material component RK tetraisopropyl orthotitanate is dissolved in commercial gasoline (ROZ 95) as raw material component RK. The raw material mixture RG in the form of a raw material solution thus formed has a metal content of 5% titanium. The raw material batch RG is at a throughput of 10 kg / h with the help of a hose pump in the combustion chamber inlet opening 9.4 of in 3 shown thermal reactor 1 or in the feed point 5.2 of in 4 shown thermal reactor 1 pumped and there periodically dusted via a valve with a frequency of 40 Hz in the hot gas stream HGS and in the thermal reactor 1 thermally treated. In addition, the task of combustion air VL takes place via the combustion chamber inlet opening 9.1 in the combustion chamber 8th , The hot gas flow HGS is by adding the cooling medium KM cooling air at the feed point 5.3 or 5.4 ( 4 ) in the front or middle part of the reaction space 2 cooled so that the temperature behind the feed point 5.3 or 5.4 the cooling air (based on the hot gas flow) is reduced to 300 ° C.

Reactor parameters:

• - Temperature in the combustion chamber 8th : 750 ° C

As a filter 7 For separating the finely divided particles P from the hot gas flow HGS, a cassette filter is used. The TiO ₂ particles P have a particle size of d 50 = 30 nm, a spherical particle shape and a specific surface area (BET) of 37 m ² / g.

Example 2)

The raw material component RK zinc acetate is dissolved in the raw material component RK water as a solvent with heating (30-50 ° C), so that the resulting raw material batch RG in the form of a raw material solution has a metal content of 12% ZnO. For defined adjustment of the resulting powder properties, such as UV absorptivity, the raw material batch RG may comprise further customary doping elements as raw material components RK. This raw material mixture RG is at a throughput of 100 kg / h using a peristaltic pump in the reaction chamber 2 at the feed point 5.2 of in 5 shown reactor 1 pumped and continuously dusted there via a 1.8 mm titanium nozzle in the hot gas stream HGS and thermally treated.

The pulsating hot gas flow HGS (20 Hz) is due to the discontinuous application of natural gas as energy source ET in the combustion chamber 8th at the combustion chamber inlet opening 9.2 generated. The temperature of the generated hot gas flow HGS is by supplying cooling air as the cooling medium KM at the feed point 5.1 so reduced that in the reaction space 2 set a process temperature of 600 ° C.

Reactor parameters:

• - Temperature in the combustion chamber 8th : 1000 ° C
• - Temperature in the reaction space 2 : 600 ° C

As a filter 7 For separating the finely divided particles P from the hot gas flow HGS, a cassette filter is used. The ZnO particles P have a particle size of d50 = 25 nm, a spherical particle shape and a specific surface area (BET) of 44 m ² / g.

Example 3)

Analogous to the embodiment 2 For example, finely divided ZnO powder is prepared from Zn acetate dissolved in water as raw material component RK as raw material component RK. In this embodiment, however, the hot gas flow HGS with the particles P formed therein becomes out of the reaction space 2 in another reaction room 2 ' (not shown).

At the feed point 5.2 ' (not shown) is additionally gaseous tetraethoxy orthosilicate (TEOS) injected as a coating amount BG in the reaction space 2 ' initiated. The injected volume of gaseous TEOS is chosen so that the molar ratio TEOS to injected zinc acetate is 1/10. The resulting silicon dioxide encases the zinc oxide particles P in the hot gas stream HGS, and in addition to the coated zinc oxide particles P, a small proportion of pure SiO ₂ particles P is formed as a product.

Reactor parameters:

• - Temperature in the combustion chamber 8th : 1000 ° C
• - Temperature in the reaction space 2 : 600 ° C
• - Temperature in the reaction space 2 ' , 575 ° C

As a filter 7 For separating the finely divided particles P from the hot gas flow HGS, a cassette filter is used. The SiO ₂ coated ZnO particles P (composite material) have a particle size of d ₅₀ = 50 nm, a spherical particle shape and a specific surface area (BET) of 25 m ² / g.

Example 4)

To prepare the exemplary embodiment, aluminum tri-sec-butoxide is initially dissolved as raw-material component RK in isopropanol as raw-material component RK with stirring (solution A). The dissolution of dried yttrium acetate as raw material component RK and cerium (III) nitrate as raw material component RK takes place separately with stirring in the raw material components RK DMSO (solution B). Alternatively, further doping elements can be added as raw material components RK or replace the elements used. Solution A is added with stirring to solution B. The Y-Al-Ce mixed nitrate solution (solution C) corresponds to the molar ratio 2.91: 5: 0.09 for the elements Y, Al and Ce.

This Solution C becomes petroleum benzine as raw material component RK added in a ratio of 1: 1. To stabilize took place the addition of auxiliary components (Span 80, Span 40). From this mixture The treatment in a homogenizer becomes a mixture of raw materials RG made in the form of an emulsion The raw material batch RG then becomes Homogenized ten times in a high-pressure homogenizer at 200 kbar.

The raw material batch RG is at a throughput of 50 kg / h using a peristaltic pump in the combustion chamber inlet opening 9.4 of in 3 shown thermal reactor 1 pumped and there periodically dusted via a valve with a frequency of 50 Hz in the hot gas stream HGS and in the reactor 1 thermally treated. In addition, the task of combustion air VL takes place via the feed point 9.1 in the combustion chamber 8th ,

Reactor parameters:

• - Temperature in the combustion chamber 8th : 900 ° C
• - Temperature in the reaction space 2 : 850 ° C

As a filter 7 For separating the finely divided particles P from the hot gas flow HGS a bag filter is used. The YAG: Ce particles P have a particularly high homogeneous element distribution. The grain size is d ₅₀ = 700 nm, with a spherical particle shape and a specific surface area (BET) of 6 m ² / g.

1

thermal reactor

2, 2 '

reaction chamber

3

Hot gas inlet

4

first Valve

5

supply point

6

outlet

7

filter

8th

combustion chamber

9

Combustion chamber inlet port

10

ignition source

11

piston

12

second Valve

BG

coating mixture

ET

fuels

GK

Further gaseous component

HGS

Hot gas stream

KM

cooling medium

P

particle

RG

raw material mixture

RK

raw material component

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• WO 02/072471 [0006]
• - DE 102004044266 A1 [0006]

Claims (42)

Thermal reactor ( 1 ) for the production of particles (P) comprising at least one reaction space ( 2 . 2 ' ), wherein one of the reaction spaces ( 2 . 2 ' ) through a hot gas inlet ( 3 ) periodically a hot gas stream (HGS) can be fed and wherein this reaction space ( 2 . 2 ' ) in addition a raw material batch (RG) can be supplied and wherein at least one raw material component (RK) of the raw material mixture (RG) formed particles (P) by an outlet ( 6 ) from this reaction space ( 2 . 2 ' ) leachable or another of the reaction spaces ( 2 . 2 ' ) and wherein a frequency of the periodic supply of the hot gas stream (HGS) by at least one controllable first valve ( 4 ) at the hot gas inlet ( 3 ) or preceded by this and / or by a periodic combustion of at least one hot gas stream (HGS) forming energy carrier (ET) and / or at least one of the energy carrier (ET) used, the hot gas flow (HGS) forming raw material components (RK) with controllable combustion frequency in at least one hot gas inlet ( 3 ) upstream combustion chamber ( 8th ) can be specified. Thermal reactor ( 1 ) according to claim 1, wherein the raw material mixture together with the hot gas stream (HGS) through the hot gas inlet ( 3 ) or separately by at least one feed point ( 5.1 to 5.n ) can be fed. Thermal reactor ( 1 ) according to claim 1 or 2, characterized in that one of the reaction spaces ( 2 ) a filter ( 7 ) downstream of the separation of the particles (P) from the hot gas stream (HGS). Thermal reactor ( 1 ) according to one of claims 1 to 3, characterized in that the combustion chamber ( 8th ) is designed as an internal combustion engine. Thermal reactor ( 1 ) according to one of claims 1 to 4, characterized in that the combustion chamber ( 8th ) at least one combustion chamber inlet opening ( 9.1 to 9.n. ) for supplying the energy carrier (ET) and / or the raw material mixture (RG) and / or at least one further gaseous component (GK). Thermal reactor ( 1 ) according to one of claims 1 to 5, characterized in that the combustion of the energy carrier (ET) by means of auto-ignition by high pressure and / or high temperature and / or by means of a continuously and / or periodically activated ignition source ( 10 ) is initiatable. Thermal reactor ( 1 ) according to claim 6, characterized in that as ignition source ( 10 ) a pilot flame and / or a glow plug and / or a spark plug and / or at least one glow wire and / or a Glühgitter in the combustion chamber ( 8th ) is arranged. Thermal reactor ( 1 ) according to one of claims 3 to 7, characterized in that the combustion chamber inlet opening ( 9.1 to 9.n. ) as a nozzle and / or as a second valve ( 12 ) and / or is designed as a solenoid valve. Thermal reactor ( 1 ) according to claim 8, characterized in that a pressure applied to the nozzle is adjustable. Thermal reactor ( 1 ) according to one of claims 1 to 9, characterized in that in the combustion chamber ( 8th ) at least one flow element for turbulence of the raw material mixture (RG) and / or the energy carrier (ET) is arranged. Thermal reactor ( 1 ) according to one of claims 3 to 10, characterized in that the combustion chamber inlet opening ( 9.1 to 9.n. ) is preceded by a mixing chamber and / or the combustion chamber inlet opening ( 9.1 to 9.n. ) is formed as a mixing nozzle. Thermal reactor ( 1 ) according to one of claims 1 to 11, characterized in that the frequency of the periodic supply of the hot gas stream (HGS) or the combustion frequency in a range of 3 Hz to 200 Hz is adjustable. Thermal reactor ( 1 ) according to one of claims 1 to 12, characterized in that at least one of the reaction spaces ( 2 . 2 ' ) is usable as a drying room and / or as a calcining room and / or as a phase transformation room. Thermal reactor ( 1 ) according to one of claims 1 to 13, characterized in that the to the combustion chamber ( 8th ) subsequent reaction space ( 2 ) tube-like and / or with a conical hot gas inlet ( 3 ) and / or with a conical outlet ( 6 ) is formed. Thermal reactor ( 1 ) according to one of claims 3 to 14, characterized in that the filter ( 7 ) is designed as a gas cyclone or as a hot gas filter or as a surface filter or as an electrostatic precipitator or as a bag filter. Process for the production of particles (P) in at least one reaction space ( 2 . 2 ' ) comprehensive thermal reactor ( 1 ), in which at least one hot gas stream (HGS) one of the reaction spaces ( 2 . 2 ' ) through a hot gas inlet ( 3 ) is supplied periodically, the reaction space ( 2 . 2 ' ) together with the hot gas stream (HGS) through the hot gas inlet ( 3 ) or separately by at least one feed point ( 5.1 to 5.n ) a raw material mixture (RG) is supplied, which comprises at least one raw material component (RK), wherein in the hot gas stream (HGS) from at least one of the raw material components (RK) particles (P) are formed, which through an outlet ( 6 ) from this reaction space ( 2 . 2 ' ) or another of the reaction spaces ( 2 . 2 ' ), wherein a frequency of the periodic supply of the hot gas flow (HGS) by at least one controllable first valve ( 4 ) at the hot gas inlet ( 3 ) or preceded by this and / or by a periodic combustion of at least one energy carrier (ET) and / or at least one of the raw material components (RK) with controllable combustion frequency used as energy carrier (ET) in at least one hot gas inlet ( 3 ) upstream combustion chamber ( 8th ) is given. Method according to claim 16, characterized in that that as an energy source (ET) or as one of the raw material components (RK) a high-calorie solid and / or a high-calorie Liquid and / or a high calorific gas is used. Method according to one of claims 16 or 17, characterized in that at least one of the raw material components (RK) is used as an auxiliary component. Method according to claim 18, characterized that the raw material batch (RG) with the help of as solvent trained auxiliary component to a raw material solution conditioned becomes. Method according to claim 19, characterized that the raw material mixture (RG) with the help of trained as a dispersant Auxiliary component is conditioned to a raw material dispersion. Method according to one of claims 18 to 20, characterized in that as an auxiliary component an organic Fabric is used. Method according to one of claims 16 to 21, characterized in that the combustion of the energy carrier (ET) by means of auto-ignition by high pressure and / or high temperature and / or by means of a continuously and / or periodically activated ignition source ( 10 ) is initiated. Method according to claim 22, characterized in that as ignition source ( 10 ) a pilot flame and / or a glow plug and / or a spark plug and / or at least one glow wire and / or a Glühgitter is used. Method according to one of claims 16 to 23, characterized in that the supply of the energy carrier (ET) and / or the raw material mixture (RG) and / or at least one further gaseous component (GK) into the combustion chamber ( 8th ) via at least one as a nozzle and / or as a second valve ( 12 ) and / or formed as a solenoid valve combustion chamber inlet opening ( 9.1 to 9.n. ) is controlled. Method according to Claim 24, characterized a pressure applied to the nozzle for adjustment a droplet size is varied. Method according to one of claims 24 or 25, characterized in that as a further gaseous component (GK) air and / or oxygen and / or carbon dioxide is used. Method according to one of claims 24 to 26, characterized in that a mixture of the raw material mixture (RG) and / or the energy carrier (ET) and / or the further gaseous component (GK) in one of the combustion chamber inlet opening ( 9.1 to 9.n. ) upstream Mischkam mer or the combustion chamber inlet opening ( 9.1 to 9.n. ) forming mixing nozzle takes place. Method according to one of claims 16 to 27, characterized in that the frequency of the periodic feed of the hot gas flow (HGS) or the combustion frequency in a range of 3 Hz to 200 Hz is set. Method according to one of claims 16 to 28, characterized in that after the particle formation a drying and / or calcination and / or a phase transformation and / or an at least partial coating in at least one of the further reaction spaces ( 2 . 2 ' ) takes place. Method according to one of claims 16 to 29, characterized in that the supply of the raw material mixture (RG) into the combustion chamber ( 8th ) and / or into the reaction space ( 2 . 2 ' ) and / or the supply of the energy carrier (ET) and / or the further gaseous component (GK) into the combustion chamber ( 8th ) occurs periodically and / or continuously. Method according to one of claims 16 to 30, characterized in that the raw material mixture (RG) in solid form and / or introduced as solution and / or as a dispersion and / or gaseous and / or sprayed and / or atomized and or by means of a downpipe in the combustion chamber ( 8th ) and / or into the reaction space ( 2 . 2 ' ) is introduced. A method according to claim 31, characterized ge indicates that the raw material batch (RG) or at least one of the raw material components (RK) are transferred to the gas phase before being introduced. Method according to one of claims 31 or 32, characterized in that the introduction of the raw material mixture (RG) with or against a flow sense of the hot gas stream (HGS) takes place. Method according to one of claims 16 to 33, characterized in that as raw material component (RK) at least an organic or inorganic substance from the group of nitrates, Chlorites, carbonates, bicarbonates, carboxylates, alcoholates, Acetates, oxalates, citrates, halides, sulfates, organometallic Compounds or hydroxides is used. Method according to one of claims 16 to 34, characterized in that the raw material mix (RG) is a or multi-stage wet-chemical intermediate step. Method according to one of claims 16 to 35, characterized in that a temperature profile of the hot gas stream (HGS) at least in parts of the thermal reactor ( 1 ) is controlled and / or regulated. Method according to Claim 36, characterized that a maximum temperature of the hot gas in a range from 200 ° C to 2000 ° C is performed. Method according to one of the claims 36 or 37 , characterized in that the temperature profile by abandonment of a further energy carrier (ET) and / or task of a cooling medium (KM) at at least one further feed point ( 5.1 to 5.n ) is controlled and / or regulated. Method according to one of claims 19 to 38, characterized in that the coating at least one organic and / or inorganic gaseous and / or liquid Coating Amount (BG) is used. Method according to one of claims 16 to 39, characterized in that at least one single or multi-stage thermal aftertreatment of the particles (P) in another thermal Reactor takes place. Method according to claim 40, characterized in that that before and / or during the thermal aftertreatment a further at least partial coating takes place. Method according to one of claims 40 or 41, characterized in that before, during or after the thermal aftertreatment, dry grinding and / or transfer the particle (P) in a suspension and / or a wet grinding and / or a drying of the suspension takes place.