KR20170010805A - Combustion of lithium at different temperatures and pressures and with gas surpluses using porous tubes as burners - Google Patents

Abstract

The present invention relates to a method for burning a metal (M) selected from alkali, alkaline earth metals, aluminum, and zinc, and alloys and / or mixtures thereof, using fuel gas. The combustion is carried out by means of a porous burner 3 comprising a porous tube as a burner. The invention also relates to the use of a device for carrying out the process and a porous burner comprising a porous tube as a burner for burning metal (M) using combustion gases.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and apparatus for burning lithium by using porous tubes as burners at different temperatures and pressures and using gas surpluses. BACKGROUND OF THE INVENTION < RTI ID = 0.0 > [0002] <

The present invention relates to a process for the production of a metal (M) selected from the group consisting of alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / - combustion is carried out by means of a pore burner comprising a porous tube as a burner, - an apparatus for carrying out the process, and - To a use of a pore burner comprising a porous tube as a burner for combustion of a metal (M) selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / or mixtures thereof.

Over the years, a number of energy generation units have been proposed for working with heat generated from the oxidation of metallic lithium (see, for example, U.S. Patent No. 33 28 957). In this system, water and lithium react with each other to produce lithium hydroxide, hydrogen, and steam. Elsewhere in the system, hydrogen generated by the reaction between lithium and water is combined with oxygen to form additional steam. Next, the steam is used to drive a turbine or the like, and thus an energy generation source is obtained. Lithium may also be used additionally to obtain commodity materials. For example, by reacting with nitrogen to provide lithium nitride and then hydrolyzed to provide ammonia or react with carbon dioxide to provide lithium oxide and carbon monoxide. As in the case of nitrides, in each case, optionally after hydrolysis, the final end product of the solids of the reaction of lithium is an oxide or carbonate, which is then reduced again by electrolysis to lithium metal . This can be achieved by establishing circuits in which surplus power can be generated, stored and converted back to power at a desired time by wind power, photovoltaic cells or other renewable energy sources, or else chemical raw materials can be obtained.

Lithium is typically produced by melt-flow electrolysis. For this process, efficiencies of about 42% to 55%, calculated from process data without temperature correction of the standard potential, were identified. It is also possible to use not only lithium but also similar metals such as sodium, potassium, magnesium, calcium, aluminum and zinc.

Particular attention should be given to these because solid or liquid residues can occur in the combustion of lithium depending on the temperature and the fuel gas. Moreover, depending on the configuration and operation of the oven for combustion of lithium metal in different atmospheres and under pressure (e.g. in liquid form), offgas and solids / liquids can be generated as combustion products have. These solid and liquid materials must be very substantially separated from the offgas.

It is important to substantially completely separate the liquid and solid combustion residues from the offgas stream so as not to generate any surface deposits or occlusions in downstream devices. More specifically, it is highly desirable to direct the off-gas stream directly to the gas turbine, since in that case it must be ensured that all particles have been completely removed from the off-gas stream. These particles cause long term damage to gas turbine blades and cause plant disruption.

It is an object of the present invention to provide a process for the production of solid and / or gas from offgas in the case of combustion of a metal (M) selected from alkali metals, alkaline earth metals, Al and Zn, Or liquid reaction products can be carried out in the process of the present invention. It is a further object of the present invention to provide a method and system for the efficient and locally limited combustion of a metal (M) using fuel gas, without the need for too much distribution of the combustion products in the combustion space, And to provide a device that can be used. Furthermore, an object of the present invention is to effectively control the combustion of the metal (M) using the fuel gas.

This object is achieved by the use of a pore burner comprising a porous tube as a burner in the combustion of metal (M) using fuel gas. Through the use of pore burners it has been found possible to localize the combustion in a pore burner, in which case the combustion products are also obtained in the pore burner. On the other hand, for example, in the case of atomization, reaction products are obtained throughout the reactor, the solid and liquid reaction products must be separated again from the gas reaction products in a complicated manner, and in the case of combustion using a pore burner, There is localization of the solid and liquid reaction products particularly close to that which facilitates the separation of the solid and liquid reaction products from the gaseous combustion products. In this way, the entire combustion device can also be made more compact, and the combustion can be configured to be gentler with respect to the device through localization of the combustion process.

In a first aspect, the present invention relates to a process for burning a metal (M) using a fuel gas, wherein the metal (M) is selected from the group consisting of alkali metals, alkaline earth metals, aluminum and zinc, / ≪ / RTI > mixtures, and the combustion is carried out by a pore burner comprising a porous tube as a burner.

In a further aspect, the invention relates to an apparatus for the combustion of a metal (M), wherein the metal (M) is selected from the group consisting of alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / The apparatus comprises a pore burner comprising a porous tube as a burner, a feed unit for the metal (M), preferably in the form of a liquid, into the interior of the pore burner, preferably a feed A feed unit designed for feeding fuel gas, a feed unit for the fuel gas, and optionally a heating device for providing the metal (M) in liquid form , And the heating device is designed to liquefy the metal (M).

In addition, the present invention provides, in a further aspect, a burner for burning a metal (M) selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / To a pore burner comprising a porous tube.

Further aspects of the invention can be deduced from the dependent claims and the more detailed description, and also from the drawings.

The accompanying drawings are intended to illustrate embodiments of the invention and to provide a further understanding of the invention. In the context of the description, the appended drawings serve to explain the principles and concepts of the present invention. Many other embodiments and the advantages mentioned will become apparent with reference to the drawings. The elements of the figures are not necessarily to scale with respect to each other. The same elements, features, and components having the same function and the same effect are given the same reference numerals in the drawings of the drawings, respectively, unless otherwise stated.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 shows in an overview form an exemplary arrangement for the apparatus of the present invention.
Figure 2 shows in a schematic form a detailed view of a further exemplary arrangement for an apparatus of the present invention.
Figure 3 shows in further detail a further detail of an additional exemplary arrangement for the apparatus of the present invention.
Figure 4 schematically illustrates an exemplary cross-section through an exemplary apparatus of the present invention in the region of the feed unit of carrier gas to the reactor.
Figure 5 shows a scheme for an exemplary reaction of lithium and carbon dioxide to provide lithium carbonate, which may be carried out by a process according to the present invention.
Figure 6 shows a scheme for further exemplary reaction of lithium and nitrogen to provide lithium nitride and further conversion products, which may be implemented by the process according to the present invention.

In a first aspect, the present invention relates to a process for burning a metal (M) using a fuel gas, wherein the metal (M) is selected from the group consisting of alkali metals, alkaline earth metals, aluminum and zinc, Or mixtures, and the combustion is carried out by a pore burner comprising a porous tube as a burner.

In certain embodiments, the metal (M) is selected from the group consisting of alkali metals, preferably Li, Na, K, Rb and Cs, alkaline earth metals, preferably Mg, Ca, Sr and Ba, Al, Mixtures thereof and / or alloys thereof. In a preferred embodiment, the metal M is selected from Li, Na, K, Mg, Ca, Al and Zn, more preferably Li and Mg, and the metal M is more preferably lithium.

In certain embodiments, useful fuel gasses are those that are capable of reacting with mixtures and / or alloys of the aforementioned metals (M) or metals (M) in an exothermic reaction, It does not. By way of example, the fuel gas may comprise air, the oxygen, carbon dioxide, hydrogen, water vapor, nitrogen oxides, NO _x, for example, dinitrogen monoxide, nitrogen, sulfur dioxide, or mixtures thereof. Thus, the process can also be used for desulfurization or NO _x removal. According to the fuel gas, it is possible here to obtain various products which may be in solid, liquid, or otherwise gaseous form using various metals M. [

For example, the reaction of a metal (M) such as lithium with nitrogen may result in, in particular, a metal nitride, such as lithium nitride, which, in turn, may be allowed to react further at a later stage to provide ammonia , Metal (M), such as lithium and carbon dioxide, can lead to, for example, metal carbonates such as lithium carbonate, carbon monoxide, metal oxides such as lithium oxides, otherwise metal carbides such as lithium carbide, For example, longer-chain carbonaceous products such as methane, ethane and the like, as well as benzene, diesel as well as methanol, etc., in the Fischer-Tropsch process, While it is possible to use carbon monoxide to obtain high-value products, for example, to obtain acetylene Year, it is possible to use a metal carbide, such as lithium carbide. In addition, it is also possible to use, for example, dinitrogen monoxide as a fuel gas to form a metal nitride, for example.

Similar reactions may also occur for other metals mentioned.

According to the present invention, if a pore burner includes a porous tube as a burner, in which the metal M can be fed from at least one orifice, the pore burner is not particularly limited. Preferably, the metal (M) is fed only through one orifice of the tube and the other end of the tube is closed or similarly made of the material of the porous tube. The porous tube may here be a ceramic tube made of, for example, aluminum oxide or magnesium oxide, or an alloy of these metals, such as iron, chromium, nickel, niobium, tantalum, molybdenum, tungsten, zirconium, , Stainless steel, and porous metal tubes made of chrome-nickel steel. The pore burner is preferably a material selected from the group consisting of iron, chromium, nickel, niobium, tantalum, molybdenum, tungsten, zirconium and alloys of these metals and also steels such as stainless steel and chromium- . Suitable examples are, for example, austenitic chromium-nickel steels which are highly resistant to sodium corrosion at elevated temperatures, but are not limited to AC 66, Incoloy 800 or Pyrosom G 20132 Nb (Pyrotherm G 20132 Nb), 32% nickel and 20% chromium also exhibit relatively favorable corrosion properties. The additional components of the pore burner are not subject to any further restrictions and may include a feed unit for the metal M and optionally an ignition source and the like.

In certain embodiments, the metal (M) is guided to the pore burner in the liquid form and burned with the aid of a pore burner, the fuel gas is optionally directed to the outer surfaces of the pore burner, Burned. However, in certain embodiments, no internal mixing occurs, such as in conventional pore burners, to avoid clogging of pores by solid reaction products. In certain embodiments, the pore burner is thus a pore burner that does not have an internal mix. In certain embodiments, in the case of the use of a pore burner, the pores merely serve to increase the surface area of the alloy (L). However, in the case of continuous feeding of an alloy (L) of a positive metal, the reaction with the fuel gas can be carried out in the following manner, if the reaction products formed can be ensured to be delivered out of the pore burner by the further transfer of the alloy (L) Can occur at the exit of pores near the surface of the pore burner. However, in certain embodiments, the combustion reaction is carried out only at the outside of the pores of the pore burner, for example at the surface of the pore burner, or even after the release of the alloy L from the pore burner, Occurs.

In certain embodiments, the pore burner is supplied with a metal (M) in liquid form inside the pore burner. This results in a better distribution of the metal (M) in the pore burner and a more homogeneous discharge of the metal from the pores of the porous tube, resulting in a more homogeneous reaction between the metal (M) and the fuel gas. The combustion of the metal (M) and the fuel gas can be effected, for example, by correlating the pore size of the pores of the tube, the metal (M) used, the density thereof with the temperature of the metal (M) The pressure entering the burner, the pressure of the fuel gas or the application / feed rate. In certain embodiments, the metal (M), e.g., lithium, is used in a correspondingly liquid form, i. E., Above the melting point of lithium, e. Here, for example, the liquid metal M can also be injected into the porous tube using the help of additional gas under pressure, which is not limited. The liquid metal M is then delivered to the surface through the pores of the tube and is burned using gas to provide the respective reaction product (s).

In certain embodiments, the fuel gas is directed to the outer surfaces of the pore burner and burned with the metal (M). This can reduce or prevent clogging of the pores of the porous tube, thereby preventing cleaning of the pore burner or otherwise reducing wear.

The combustion of the metal (M) at the surface of the porous tube reduces the tendency for the passage of small particles into the gas space / reaction space, so that at most, relatively large droplets of reaction products are generated, Can be easily separated, and can be deposited on the reactor wall, for example, by a cyclone. In this case, the reactor wall can be cooled, for example using heat exchangers, in which case the heat exchangers can also be connected to the turbines and generators.

In certain embodiments, the combustion is conducted at a temperature that exceeds the melting point of the salts formed in the reaction of the metal (M) and the fuel gas. The salts formed in the combustion of the metal (M) and the fuel gas may here have a melting point exceeding the melting point of the metal (M), so that the supply of the liquid metal (M) at an elevated temperature may be required. Combustion at temperatures above the melting point of the formed salts can additionally avoid contamination or coverage of the pore burner by the formed salts so that the pore burner can be better protected against contamination of the pores, . This allows for better operation and reduced cleaning of the device and also longer usage times without cleaning. It is also possible that the liquid reaction product simply falls off the burner. In the case of such processes at temperatures exceeding the melting point of the salts formed, the preferred materials for the burner in particular are those which are capable of withstanding these temperatures, such as iron, niobium, tantalum, molybdenum, tungsten, zirconium, Alloys and stainless steel.

Thus, the combustion temperature is preferably higher than the melting point of the respective reaction product (s), so that the pores of the pore burner are not obstructed and the reaction products can be transported away. In addition, depending on the reaction product, a certain degree of mixing may occur between the liquid metal (M) and the reaction product, so that combustion may occur locally in the pore openings as well as throughout the entire surface of the tube. This can be controlled, for example, via the feed rate of the metal (M).

In certain embodiments, the metal (M) is supplied to the pore burner as an alloy of at least two metals (M). In this way it is possible to achieve a lowering of the melting point of the metal (M) and also of the formed metal salt (s), so that the process can be carried out at lower temperatures, The use of highly refractory materials in the device can be reduced or avoided.

In addition, in certain embodiments, to stabilize the off-gas temperature within a certain temperature range, a certain excess amount of fuel gas may be introduced into the fuel gas, for example, 1.01: 1 or more, preferably 1.05: 1 or more, More preferably a molar ratio of fuel gas to metal (M) of 5: 1 or more, even more preferably of 10: 1 or more, such as even 100: 1 or more. Can be implemented. The fuel gas may also serve here for the removal of heat at the inflator portion, such as a turbine.

In the process, in the case of the combustion of the metal (M) using the fuel gas, the separation of the offgas from the solid and / or liquid reaction products can additionally be carried out, in which case, in certain embodiments, In the reaction step, the fuel gas is burned with the metal (M), off-gas and further solid and / or liquid reaction products are formed, and in the separation step, the off gas is separated from the solid and / or liquid reaction products . In this case, in the separation step, an additional carrier gas may be added, and the carrier gas may be removed as a mixture with the offgas. Here, the carrier gas may also correspond, for example, to off-gas resulting in off-gas corresponding to the supplied carrier gas, or otherwise to a fuel gas. Thus, in the process of the present invention, in certain embodiments, it is possible to separate reaction products after combustion.

According to the present invention, the carrier gas is not particularly limited and may correspond to the fuel gas, but may also be different from the fuel gas. The carrier gases used may be, for example, air, carbon monoxide, carbon dioxide, oxygen, methane, hydrogen, water vapor, nitrogen, dinitrogen monoxide, mixtures of two or more of these gases, It is now possible for various gases such as methane to serve for heat transfer and to remove the reaction heat of the reaction of the metal (M) and the fuel gas from the reactor. The various carrier gases may be suitably matched to the reaction of the fuel gas and the metal M, for example, possibly to achieve synergistic effects here. The gas selectively used in the supply of the metal (M) can likewise correspond to the carrier gas.

When carbon monoxide can be formed in the combustion of carbon dioxide and metal (M), for example lithium, the carrier gas used can be, for example, carbon monoxide and can optionally be circulated, Can be partially recirculated again. In this case, the carrier gas is matched to off-gas so that a portion of the carrier gas can be selectively recovered, for example, as a valuable product for subsequent Fischer-Tropsch synthesis, while the carrier gas is burned Based on the carbon dioxide used, preferably up to 90 vol% or more, more preferably up to 95 vol% or more, even more preferably up to 99 vol% or more, based on the carbon dioxide used, And particularly preferably to the extent of 100% by volume, there is at least partial conversion of the carbon dioxide to carbon monoxide as a whole and is recovered as a valuable product. The more carbon monoxide is generated, the cleaner the carbon monoxide is removed.

In the case of the combustion of nitrogen and metal (M), for example lithium, the carrier gas used can be, for example, nitrogen, so that unreacted nitrogen in the off-gas from the combustion is "offgas" with the nitrogen carrier gas As a result, the separation of the gases can be carried out in a simpler manner, if desired, and can be carried out in a suitable and suitable manner with the use of appropriate and readily determinable parameters of metals (M) and nitrogen May not even be required in the case of quantitative combustion. For example, it is possible to easily remove ammonia from the nitride formed by scrubbing or cooling.

In certain embodiments, at least a portion of the off-gas may correspond to a carrier gas. For example, based on the total volume of offgas, the offgas may be at least 10 vol%, preferably 50 vol% or more, more preferably 60 vol% or more, even more preferably 70 vol% , And even more preferably up to 80% by volume or more of the carrier gas. In certain embodiments, the fuel gas may correspond to a carrier gas to an extent of 90 vol% or more based on the total volume of the off gas, and in some cases may correspond to a carrier gas to an extent of even 100 vol% have.

In certain embodiments, in the process of the present invention, the mixture of off-gas and carrier gas may be fed at least partially back into the separation step as a carrier gas and / or as a fuel gas to the combustion step. The recycle of the mixture of offgas and carrier gas can be, for example, 10 vol% or more, preferably 50 vol% or more, more preferably 60 vol% or more, based on the total volume of the carrier gas and offgas, , Even more preferably greater than or equal to 70 vol%, and even more preferably greater than or equal to 80 vol%. In certain embodiments, the recycle of the mixture of offgas and carrier gas may be conducted to an extent of 90 vol% or more based on the total volume of carrier gas and offgas. In the preferred embodiments according to the present invention, the formed off-gas is a carrier gas, for example, the reaction between the fuel gas and the metal M can be carried out in such a manner that carbon dioxide is used as the fuel gas and carbon monoxide as the carrier gas, The mixture of the carrier gas and the off gas is then essentially purified, based on the mixture of the off gas and the carrier gas, preferably to an extent of 90 vol% or more, more preferably to a degree of 95 vol% , Even more preferably up to about 99% by volume or more, and more preferably up to about 100% by volume of the carrier gas. In this case, the carrier gas may then be continuously circulated and recovered in such an amount as is modified by the combustion of the metal (M) and the fuel gas. It is now possible to obtain a valuable product, such as carbon monoxide, which can be subsequently recovered, when the separation of the carrier gas and the off gas is selectively carried out as compared to the pure circulation of the carrier gas.

In certain embodiments, the separation step of the process of the present invention is carried out in a cyclone or cyclone reactor. The cyclone reactor is not particularly limited in terms of the setup of the cyclone reactor herein, and may have the form, for example, as possessed by standard cyclone reactors.

For example, a cyclone reactor may be connected to feed units for fuel gas, metal (M), and carrier gas (which may optionally also be pre-combined and then fed together into a reaction zone) For the solid and / or liquid reaction products from the combustion of the metal (M) by means of a fuel gas, a reaction zone in the form of a rotationally symmetric upper section, for example a separation zone with a conical configuration, an expansion chamber in the form of a star feeder and an elimination unit for a mixture of two gases occurring after the mixing of the offgas and the carrier gas after the combustion of the metal M in the fuel gas, ).

These device components are typically present, for example, in cyclone separators. The cyclone reactor used in accordance with the present invention may alternatively have different configurations and may optionally also include additional zones. For example, individual zones (e.g., reaction zones, separation zones, expansion chambers) may also be combined in one component of the exemplary cyclone reactor and / or extend across two or more components of the cyclone reactor . Here, for example, it is also possible that the carrier gas is also undergoing the reaction of the metal M with the fuel gas or even added to the already completed zone.

Because of the cyclones, the reaction products are generally held in the center of the reactor, e.g., the furnace space, and the combustion at the surface of the porous tube does not result in any small particles, such as in the case of atomization, It is also possible to connect to the downstream gas turbine or the inflator turbine in the off-gas stream, since they have no solid or liquid particles. Under these circumstances, using this combustion concept, it is possible to introduce the off-gas stream directly into the gas turbine after combustion of the metal (M) and separation of the reaction products.

In certain embodiments, the off-gas temperature can be controlled through an excess amount of gas in the different combustion processes such that the off-gas temperature is higher than the melting temperature of the reaction products or mixtures thereof.

In certain embodiments, the cyclone reactor additionally comprises a grid, wherein the solid and / or liquid reaction products can be removed from the combustion of the metal (M) by the fuel gas. These grids can additionally prevent subsequent vortexing of solid and / or liquid reaction products in the cyclone reactor.

The reaction products of combustion preferably use at least one inflator turbine and / or at least one gas turbine, such as a steam turbine, and / or at least one heat exchanger and / or at least one boiler, And for this purpose, in certain embodiments herein, for example using a reactor heat exchanger, using both formed solid and / or liquid reaction products, or otherwise using gas reaction products It is possible.

When using a cyclone reactor with a carrier gas supply, in certain embodiments, for example, a mixture of offgas and carrier gas, for example in and / or after removal from the reactor and / or from the reactor, For heat transfer, or for heat transfer in a heat exchanger or turbine, such as a gas turbine or an inflator turbine.

In addition, in certain embodiments, the mixture of carrier gas and offgas may be under elevated pressure after combustion, e.g., greater than 1 bar, at least 2 bar, at least 5 bar, or at least 20 bar.

Moreover, in a further aspect of the present invention, an apparatus is disclosed for the combustion of a metal (M) selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / or mixtures thereof,

A pore burner including a porous tube as a burner,

The feed unit-feed unit for the metal (M), preferably in the form of a liquid, into the interior of the pore burner is preferably designed to supply a metal (M) in liquid form to the pore burner,

A feed unit for fuel gas, designed to supply fuel gas, and

Optionally a heating device for providing the metal (M) in liquid form, the heating device being designed to liquefy the metal (M).

Where the pore burner can be constructed as described above. The feed unit used for the metal M may be, for example, tubes or hoses that can be heated or otherwise conveyor belts and the heating may be carried out, for example, As shown in FIG. Optionally, the feed unit for the metal (M) can also be connected to an additional feed unit for gas, optionally with a control unit such as a valve, whereby the feed of the metal (M) Lt; / RTI > Likewise, it is possible that the feed unit for the fuel gas is constituted as a tube or a hose which can be selectively heated, in which case the feed unit can be suitably determined based on the state of the gas, Lt; / RTI > It is also possible that some feed units are provided for the metal (M) or fuel gas.

In certain embodiments, the feed unit for the fuel gas is arranged so as to at least partially and preferably fully guide the fuel gas to the surface of the pore burner. This achieves an improved reaction between the metal (M) and the fuel gas.

Moreover, in preferred embodiments, the pore burner is configured so that the reaction products formed in the combustion and, optionally, the unreacted metal (M), by gravity, such as a pore burner vertically mounted in the reactor and pointing towards the surface of the earth To be removed from the surface of the pore burner. In the case of vertical arrangement of the porous combustion tubes in the furnace space, the formed liquid reaction product may flow out of the tube and then downwardly into the furnace bottom.

In this manner, unreacted, possibly dissolved, metal (M), such as lithium, in the pore burner is also burned in advance and the heat of reaction is released into the flowing fuel and carrier gases.

In certain embodiments, the pore burner is formed from a group consisting of iron, chromium, nickel, niobium, tantalum, molybdenum, tungsten, zirconium and alloys of these metals and also steels, such as stainless steel and chromium- It is made of selected material. These materials are preferred for use at relatively high temperatures, where the reaction with the liquid metal (M) and optionally with the formed liquid metal salts can occur in a simpler manner.

In certain embodiments, the apparatus of the present invention may further comprise a separation unit for the products of combustion of the metal (M), the separation unit being designed to separate the combustion products of the fuel M and of the fuel M, The separation unit is preferably a cyclone reactor.

The separating unit can serve here for the separation of the offgas in the combustion of the metal (M) using the fuel gas,

- In the reactor-reactor, a pneumatic burner is provided, a feed unit for the metal (M) is mounted or provided, and a fuel gas is supplied to the reactor, i.e., a feed unit for the fuel gas is connected to the reactor or provided at the reactor. ;

- A feed unit for the carrier gas, designed to supply a carrier gas to the reactor;

- A removal unit for a mixture of offgas and carrier gas, designed to remove the mixture of offgas and carrier gas from the combustion of metal (M) using fuel gas; And

- And a removal unit for solid and / or liquid reaction products from combustion of the metal (M) using a fuel gas, designed to remove solid and / or liquid reaction products from the combustion of the metal (M) .

The feed unit for the carrier gas is likewise not particularly limited, and it is possible to appropriately determine the feed unit for the carrier gas based on the state of the carrier gas, including for example, tubes, hoses and the like, It can also be under pressure.

If the combustion of the fuel gas and the metal M can occur in the reactor, the reactor is likewise not particularly limited. In certain embodiments, the reactor may be a cyclone reactor as shown in FIG. 1 as an example and in detail in the further embodiment of FIG. 2.

In certain embodiments, the cyclone reactor comprises feed units for fuel gas, metal (M) and carrier gas, and also reaction zones in which, for example, pore burners in the form of rotationally symmetrical upper sections can be connected, (M) in the fuel gas, for example, in the form of a shaping feeder, for solid and / or liquid reaction products from the combustion of the metal (M) And an expansion chamber to which a removal unit for a mixture of two gases occurring after the mixing of the off-gas and the carrier gas can be connected.

These device components are typically present, for example, in cyclone separators. The cyclone reactor used in accordance with the present invention may alternatively have different configurations and may optionally also include additional zones. For example, individual zones (e.g., reaction zones, separation zones, expansion chambers) may also be combined in one component of the exemplary cyclone reactor and / or extend across two or more components of the cyclone reactor .

An exemplary cyclone reactor is shown in Fig. The cyclone reactor 6 shown in Fig. 1 has a reaction zone 20a, a separation zone 20b and a separation zone 20b together with the reaction zone 20a in the upper component 6a, And with the expansion chamber 20c. A feed unit 1 for a fuel gas, for example in the form of a selectively heated tube or hose, and a feed unit 2 for a metal M, for example in the form of a selectively heated tube or hose, And the metal (M) is supplied to the pore burner (3). According to figure 1, the metal M is fed with the aid of the gas of the feed unit 2 'for the gas, e.g. tube or hose, and the feed of gas is controlled using the valve 2 " . The metal (M) and the fuel gas are fed into the reaction zone 20a. Through the feed unit 4, a carrier gas is supplied to the zone 4 'for gas distribution and then a carrier gas from the zone 4' is supplied to the nozzles, (5). Although a detailed view of such a feed unit 4 and nozzle 5 with a zone 4 'for gas distribution is shown in cross-section in Fig. 4 (an example without a pore burner 3) by way of example, It is also possible that there are more nozzles 5 at an appropriate distance in the ring around the inner wall of zone 4 'to create. The solid and / or liquid reaction products are removed from the lower component 6b comprising the expansion chamber 20c via a removal unit 7 for solid and / or liquid reaction products of combustion of the metal (M) , But the mixture of the off-gas and the carrier gas is removed through the removal unit 8 for the mixture of the off-gas and the carrier gas.

Alternatively, in the apparatus of the present invention, an ignition device, such as an electric ignition device or a plasma arc, may be required, which may depend on the nature and state of the metal (M), such as the temperature of the metal (M) Conditions, characteristics of the fuel gas, such as the pressure and / or temperature of the fuel gas, and the arrangement of the components of the apparatus, e.g., the nature and characteristics of the feed units.

(E. G., 5 bar or greater) or higher (e. G., Greater than or equal to 5 bar) and greater than < RTI ID = 0.0 > In order to achieve both operating pressures of 20 bar or more, the internal reactor material may be made of alloys of high heat resistance, such as in extreme cases even Haynes 214 material. It is then possible to arrange the thermal insulation around this material, which is assumed to withstand only high temperatures, to allow a sufficiently small amount of heat to pass, so that the steel wall on the exterior - the steel wall - Can be cooled or water-cooled - Absorbs compressive stress. The off-gas can then be fed to an additional process step at an elevated or higher operating pressure.

Furthermore, the reactor, for example the cyclone reactor, can also be heated to the reaction zone, the separation zone and / or the expansion chamber and also to the various heating and / or desorber devices, optionally a burner, and / And / or cooling devices. Moreover, additional components such as pumps for the generation of pressure, vacuum, etc. may be present in the apparatus of the present invention.

In embodiments in which the reactor takes the form of a cyclone reactor, the cyclone reactor may comprise a grid, wherein the grid is configured such that solid and / or liquid reaction products are removed through the grid during combustion of the metal (M) . Moreover, such a grid may alternatively and additionally be present in other reactors that may be provided in the apparatus of the present invention. The use of a grid in a reactor or cyclone reactor can achieve better separation of solid and / or liquid reaction products in the combustion of metal (M) from a mixture of off-gas and carrier gas. This grid is shown by way of example in Fig. 2, where the grid 6 'is present, for example, in the cyclone reactor 6 shown in Fig. 1, and on the removal unit 7 and below the removal unit 8 And is present in the lower component 6b. It is possible to ensure reliable separation of solid and liquid reaction products or mixtures thereof, preferably by a grid which is at a sufficiently large distance from the reactor wall. In this way, already deposited solid or liquid combustion products are also not vortexed by the cyclone.

If the carrier gas can be mixed with the off-gas from the combustion of the metal (M) and the fuel gas, the geometry of the feed units for the carrier gas is not particularly limited. The cyclone is preferably formed here, for example, using the apparatus shown in Fig. The cyclone may alternatively be generated by different arrangements of feed units, one with respect to the other. For example, it is not impossible for the feed unit for the carrier gas to be present on top of the reactor close to the feed units for metal (M) and fuel. Correspondingly, the appropriate geometric structures for implantation can easily be determined in an appropriate manner, for example based on flow simulations.

And the elimination units are not particularly limited, for example, it is possible for the elimination unit for the mixture of offgas and carrier gas to be constructed as a tube, while the solid and / or liquid reaction products of combustion of the metal (M) For example, as a forming feeder and / or as a tube with a siphon. It is also possible here that various valves, such as pressure valves and / or additional regulators, are provided. For example, the exemplary elimination unit 7 shown in Fig. 3 of the cyclone reactor 6 shown in Fig. 1, in this regard, comprises a siphon 9, a valve 10 for degassing, (11), but is not limited to such a removal unit. Such siphons of the solid and / or liquid reaction products for the combustion of the metal (M) by means of the fuel gas, optionally together with a supply pressure regulator suitable for the particular operating pressure, Lt; / RTI >

In certain embodiments, the removal unit for a mixture of offgas and carrier gas may also include a separation device for offgas and / or carrier gas and / or for separate components of offgas.

In certain embodiments, the removal unit for a mixture of offgas and carrier gas is configured to remove the carrier gas from the carrier gas, such that the mixture of offgas and carrier gas is fed at least partially into the reactor as a carrier gas and / And / or a feed unit for the fuel gas. Here, the ratio of the recirculated gas may be 10 vol% or more, preferably 50 vol% or more, more preferably 60 vol% or more, or even more preferably 10 vol% or more, based on the total volume of the carrier gas and the off- More preferably 70% by volume or more, and even more preferably 80% by volume or more. In certain embodiments, recirculation of the mixture of offgas and carrier gas can be accomplished to an extent of 90 vol% or more based on the total volume of carrier gas and offgas.

In certain embodiments, the apparatus of the present invention additionally includes at least one boiler and / or at least one heat exchanger and / or at least one heat exchanger, Of the gas turbine and / or at least one inflator turbine. Thus, in the apparatus of FIG. 1, including for example a cyclone reactor 6, one or more heat exchangers and / or boilers and / or gas turbines and / or inflator turbines, not shown, , To the removal unit 8 and / or to the unit connected to the removal unit 8. It is also possible that heat exchange occurs in the cyclone reactor 6 itself, for example in the reaction zones 20a and / or in the outer zones of the separation zone 20b, or alternatively in the zone of the expansion chamber 20c, In this case, corresponding heat exchangers may also be connected to the turbines for power generation in the generators.

Thus, the off-gases can be sent as a mixture with the carrier gas, for further use, for example, heating of the boiler for raising the steam, release of heat in the heat exchanger, operation of the turbine,

It is possible, for example, to use a boiler, if it is not possible to find a suitable heat exchanger by means of a suitable heat exchanger, for example, the air with the appropriate pressure is heated and directed to the gas turbine as an alternative to offgas. In certain embodiments, the manner of using the boiler may be more promising and technically simpler, since the boiler can only be implemented at lower temperatures and at elevated pressures.

With the aid of one or more heat exchangers and / or one or more boilers, it is then possible to generate electrical energy through the use of, for example, steam turbines and generators. Alternatively, it is possible for the mixture of off-gas and carrier gas to be directly directed to the turbine, for example a gas turbine or an inflator turbine, thereby producing power directly. This, however, requires very good removal of solids and / or liquid reaction products from combustion of the metal (M) and fuel gas, as can be provided in particular using a grid of reactors, in accordance with the present invention. The choice of whether a boiler or a heat exchanger is to be used may also be dependent on the plant, although it may depend, for example, on whether solid reaction products are formed or liquid reaction products are produced. In the case of liquid reaction products such as liquid Li ₂ CO ₃ , special heat exchangers may be required, for example, in the case of solid products formed, while the reactor walls may serve as heat exchangers. In the case of a corresponding separation of the mixture of offgas and carrier gas from the solid and / or liquid reaction products, direct guidance of the mixture of offgas and carrier gas to the turbine may also be possible, / Or boilers may not be required in the off-gas stream.

In certain embodiments, the apparatus of the present invention may include a withdrawal apparatus in a removal unit for a mixture of off-gas and carrier gas, and the recovery apparatus may include a feed unit for the carrier gas and / Through the connection of a removal unit for a mixture of offgas and carrier gas to the feed unit for the carrier gas and / or to the feed unit for the fuel gas , It is designed to remove a portion of the mixture of off-gas and carrier gas. This portion may be greater than 1 volume%, preferably greater than or equal to 5 volume%, and more preferably greater than or equal to 10 volume%, based on, for example, the total volume of the mixture of off-gas and carrier gas. In addition, in certain embodiments, less than or equal to 50 vol%, preferably less than or equal to 40 vol%, more preferably less than or equal to 30 vol%, more preferably less than or equal to 30 vol%, based on the total volume of the mixture of off- Preferably 20 vol% or less, can be removed from the recycled mixture of offgas and carrier gas. Next, the recovered gas may be available, for example, as a valuable product for further reactions, such as when carbon monoxide is discharged and converted to higher-value hydrocarbons in the Fischer-Tropsch process.

It is also possible that the removed solids are further converted into valuable materials. For example, metal nitrides prepared from combustion with nitrogen can be converted to ammonia and alkali by hydrolysis with water, in which case the alkali formed also acts as a scavenger for carbon dioxide and / or sulfur dioxide can do.

In a further aspect, the present invention additionally provides a burner for burning a metal (M) selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / To a pore burner comprising a porous tube.

The above embodiments, configurations and developments, if feasible, can be combined with one another as desired. Further possible configurations, improvements and implementations of the present invention also include combinations of features of the present invention that have been described above or which are described below with reference to operational examples but which are not explicitly mentioned. More specifically, those skilled in the art will also add the individual aspects to each basic form of the invention as improvements or additions.

The present invention will now be illustrated on the basis of exemplary embodiments, and the exemplary embodiments do not limit the invention in any way.

In exemplary embodiments, the metal (M), for example, lithium, is used in liquid form, i.e., above the melting point-in the case of lithium, at 180 占 폚. The liquid metal (M), for example lithium, can be introduced into the pore burner, and then directly, optionally after ignition to initiate the reaction, a specific fuel gas such as air, oxygen, carbon dioxide, sulfur dioxide, hydrogen, , Nitrogen oxides NO _x , such as dinitrogen monoxide or nitrogen. The combustion of the metal (M), for example lithium, can be accomplished in the apparatus shown in Figure 1, for example, in an amount greater than the stoichiometric amount of the fuel gas, so as not to produce excessively high off-gas temperatures. Alternatively, the fuel gas may be added in an amount less than the stoichiometric or stoichiometric amount as compared to the metal (M). After combustion, a carrier gas (e.g. nitrogen, air, carbon monoxide, carbon dioxide and ammonia), which may also correspond to the fuel gas, is diluted to reduce the temperature and to generate a cyclone for deposition of solid or liquid reaction products ). The hot off-gas stream may then be used for heating the boiler or for heat transfer in a heat exchanger, and the like.

In a second exemplary embodiment, the fuel gas used in the apparatus shown in Figure 1 may be carbon dioxide, and the carrier gas used may be carbon monoxide. The metal (M) used, for example lithium, is, for example, in liquid form, i. E. Liquid lithium enters the pore burner 3, and then reacts directly with the fuel gas. This may be the case where an electric ignition or an additional ignition burner is required.

The reaction proceeds according to the following formula:

The combustion of lithium is preferably carried out in the stoichiometric burner 3 with the amount of carbon dioxide required in stoichiometric aspects, but may be carried out in a slightly super- or substoichiometric ratio ( For example, 0.95: 1 to 1: 0.95 with respect to the ratio of CO ₂ : Li). If very little carbon dioxide is used, for example, lithium carbide can be formed, and then acetylene can be obtained therefrom.

In the second stage, in the middle of the reactor / furnace 6, in the zone 4 ', the combustion products are mixed with the carbon monoxide carrier gas blown into the reactor 6 by the nozzles 5. This results in a cyclone, in which the effect of the cyclone is that the solid and / or liquid reaction products are vortexed in the reactor wall and are mainly deposited there. Preferably, an excess amount of carrier gas is used to ensure that the heat generated through combustion is transmitted far enough. As a result, it is possible to adjust the temperature of the reactor 6 appropriately.

In the case of pure carbon dioxide combustion, the lithium carbonate formed has a melting point of 723 ° C. Liquid reaction products during combustion can be expected if the combustion temperature of the reaction products is maintained above at least 723 DEG C by mixing the carrier gas and / or the fuel gas through the feed units 1, 5. The feed units may here be used for cooling in a strong exothermic reaction so that the plant is not heated too much, and the lower temperature limit may be the melting point of the formed salts, here lithium carbonate. Lithium oxide (melting point (mp) 1570 ° C) or lithium nitride (mp 813 ° C) reacts when the cyclone is additionally operated with nitrogen other than gases other than carbon dioxide, such as air or additional gases It is also possible to form in products. After separation of the liquid and solid reaction products, which can be improved by the grid 6 ', a mixture of off-gas and carrier gas is introduced into the boiler, for example, to drive the steam turbine with the downstream generator Or for evaporation of water to operate other technical devices (e.g., heat exchangers). A mixture of the off-gas and the carrier gas cooled by this process can then be reused as a carrier gas, for example, to generate a cyclone in the furnace. Thus, the residual heat from the off-gas after the evaporation process is utilized in the boiler and only the required amount of carbon dioxide in the stoichiometric aspects for combustion with Li is consumed in the coal-fired power plants Should be obtained by off-gas cleaning.

Table 1 shows the correlation between the off-gas temperature and the stoichiometric excess for the combustion of lithium in pure carbon dioxide and the calculations were carried out with non-temperature-dependent specific heat.

Table 1: Operation of furnace as fuel gas and using carbon dioxide as carrier gas

In certain embodiments, the combustion may be performed with a certain excess amount of fuel gas, for example, greater than 1.01: 1, preferably greater than 1.05: 1, more preferably greater than 1.05: 1, to stabilize the offgas temperature within a certain temperature range Can be carried out at a molar ratio of fuel gas to metal (M) of 5: 1 or more, even more preferably of 10: 1 or more, such as even 100: 1 or more, It is possible not only to add additional fuel gas or carrier gas for absorption but also to introduce the metal (M), for example lithium, and the fuel gas in the arrangement of the nozzles as shown in Figures 1 and 4. In certain embodiments, the off-gas temperature in the different combustion processes can be controlled through an excess of gas so that the off-gas temperature can be higher than the melting temperature of the reaction products or mixtures thereof (Table 1) .

It is possible to enrich carbon monoxide in the off-gas by recirculation of the off-gas cooled by the downstream process step. In certain embodiments, it is possible to recover a portion from the off-gas and thus obtain a gas mixture of carbon monoxide and carbon dioxide having a significantly higher proportion of carbon monoxide than that specified in Table 1. [ Subsequent separation of the gas may purify the carbon monoxide to remove the carbon dioxide, and the carbon dioxide may be further used in the circulation or in the burner.

By recirculation of the CO product gas, it is possible to lower the combustion temperature in the furnace. For stoichiometric combustion, gas temperatures in excess of 3000 K can be achieved, which will result in material problems. Lowering the combustion temperature will also be possible with an excess of CO ₂ . However, this excess should be about 16 times higher than the stoichiometric amount, and therefore the CO product gas will have to be highly diluted in excess CO ₂ (concentration of only about 6% by volume). Therefore, in certain embodiments, it is reasonable to recycle a portion of the CO product gas to the burner and use it as a thermal ballast to lower the temperature. It is desirable here to set a specific reaction temperature by recycling a certain amount of the offgas and carrier gas mixture as the carrier gas. In this case, there is no formation of a CO / CO ₂ mixture which has to be separated in a complicated manner. The product gas consists mainly of CO and only small impurities of CO ₂ . In the steady state, most of the CO is cyclic, the amount of the CO removed from the circuit as modified by the positive reaction of CO ₂ and Li. For example, such circuitry may occur when CO is used as the carrier gas in a ratio of 90 vol% or more based on a mixture of off-gas and carrier gas. Thus, while a suitable amount of carbon dioxide can be supplied constantly to the combustion process, the corresponding amount of carbon monoxide can be continuously recovered from the circuit as a valuable product.

A corresponding reaction scheme is also illustrated by way of example in FIG. At CO ₂ removal 101, carbon dioxide is separated from off-gas 100 from a combustion power plant, such as, for example, a coal-fired power plant, which is then used as a carrier gas at step 102 It is burned together with lithium. This forms Li ₂ CO ₃ (103), and a mixture of carrier gas and off-gas, including CO ₂ and CO, can optionally be passed through boiler 105 after separation 104, The steam turbine 106 and hence the generator 107 are operated. There is recycle of off-gas 108 as carrier gas, and it is possible to discharge CO in step 109. [

In a third exemplary embodiment, the fuel gas and the carrier gas used in the apparatus shown in Figure 1 may be nitrogen. The metal used, for example lithium, is in the form of a liquid, e. Liquid lithium can be fed to the pore burner 3, and then reacts directly with the fuel gas. This may be the case where an electric ignition or an additional ignition burner is required.

The combustion of lithium is carried out in the pore burner 3 together with the amount of nitrogen required in stoichiometric terms, but it may be slightly stoichiometric or substoichiometric (e.g., N ₂ : 0.95: 1 to 1: 0.95 with respect to the ratio of Li).

Here the reaction is as follows:

In the second stage, in the middle part of the reactor 6, the combustion products are mixed with a carrier gas, such as nitrogen, which is injected into the reactor 6 through the nozzles 5. This results in cyclones, the effect of cyclones being that the solid and liquid reaction products are vortexed in the reactor wall, and are mainly deposited there. In the case of combustion in pure nitrogen, the formed lithium nitride has a melting point of 813 캜. Liquid reaction products during combustion can be expected if the combustion temperature of the reaction products is maintained above at least 813 DEG C by mixing the carrier gas and / or the fuel gas through the feed units 1, The feed units may here be used for cooling in a strong exothermic reaction so that the plant is not heated too much, and the lower temperature limit may be the melting point of the formed salts, here lithium-nitride. It is also possible that lithium oxide (m.p. 1570 캜) or lithium carbonate (m.p. 723 캜) is formed in the reaction products when the cyclone is operated with gases other than nitrogen, such as air or carbon dioxide or further gases. After the separation of the liquid and / or solid reaction products, which can be improved by the grid 6 ', the off-gas is introduced into the boiler, for example, to drive the turbine with the downstream generator, Is utilized for evaporation of water to operate devices (e. G., Heat exchangers). Then, the cooled off-gas after this process can be reused, for example, to generate a cyclone in the reactor 6. Thus, residual heat from the off-gas after the evaporation process is utilized in the boiler and only the amount of nitrogen required in stoichiometric aspects for combustion must be obtained, e.g., by fractionation of air.

Table 2 shows the correlation of the off-gas temperature and the stoichiometric excess for the combustion of lithium in pure nitrogen, and the calculation was carried out with non-temperature-dependent specific heat.

Table 2: Behavior of the furnace using nitrogen as the fuel gas and as the carrier gas

In certain embodiments, the combustion may be performed with a certain excess amount of fuel gas, for example, greater than 1.01: 1, preferably greater than 1.05: 1, more preferably greater than 1.05: 1, to stabilize the offgas temperature within a certain temperature range Can be carried out at a molar ratio of fuel gas to metal (M) of 5: 1 or more, even more preferably of 10: 1 or more, such as even 100: 1 or more, It is possible not only to add additional fuel gas or carrier gas for absorption but also to introduce the metal (M), for example lithium, and the fuel gas in the arrangement of the nozzles as shown in Figures 1 and 4. In certain embodiments, the off-gas temperature in the different combustion processes can be controlled through an excess of gas such that the off-gas temperature can be higher than the melting temperature of the reaction products or mixtures thereof (Table 2) .

A corresponding reaction scheme is also illustrated by way of example in FIG. Nitrogen is separated from air 200 in air fractionation 201 and then combusted with lithium in step 202 using, for example, nitrogen from air fractionation 201 as carrier gas. This forms Li ₂ N ₃ 203 and the mixture of offgas and carrier gas containing N ₂ 204 can be directed through the boiler 205 and with that help the steam turbine 206 and therefore The generator 207 is operated. There is a recycle of off-gas 208 as a carrier gas. Ammonia 210 may be obtained from lithium nitride 203 by hydrolysis 209 and LiOH 211 may be formed that is capable of reacting with carbon dioxide to provide lithium carbonate 212.

In the fourth exemplary embodiment, it may also be possible to use two reactors connected in series, for example two cyclone reactors, in the case of using air as the fuel gas, for example, in this case, The metal (M), for example lithium, and oxygen from the air can be used to produce an oxide, such as Li ₂ O, and the off-gas mainly includes nitrogen, which is then removed from the second cyclone reactor Can be reacted with a metal (M), such as lithium, as a fuel gas to provide a metal nitride, such as Li ₃ N. In this case, for example, nitrogen can act as a carrier gas, which can also be obtained from the first off-gas or, for example, if it is circulating, from the first off-gas itself.

Through the construction of the apparatus of the present invention, solid or liquid reaction products or mixtures thereof, in particular, through the use of porous combustion tubes, are separated from the formed offgas in a simple manner and are thus obtained, for example, from gas turbines or inflator turbines, , Or it is possible to send offgas for use in a boiler. In addition, in this manner, the entire combustion device can also be made more compact, and the combustion can be configured to be more gradual to the device through localization of the combustion process.

In addition, a reactor such as a furnace, such as a furnace, can be run at elevated operating pressure, and thus the combustion and deposition process can be matched to the respective conditions of the downstream stage. In certain embodiments, the possibility of a separation of the fuel gas and the carrier gas for the establishment of the cyclone enables recirculation of the off-gases after the release of heat.

Recirculation is easily possible with this configuration. Gas mixtures are also possible as fuel gas and carrier gas. By recycling the off-gas after the process step (s), it is possible to save energy and materials.

Claims (15)

A process for burning a metal (M) using a fuel gas,
The metal (M) is selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / or mixtures thereof, and the combustion is a burner, Which is carried out by a pore burner comprising a porous tube,
Process for burning metal (M) using fuel gas. The method according to claim 1,
Wherein the pore burner is supplied with the metal (M) in liquid form inside the pore burner,
Process for burning metal (M) using fuel gas. 3. The method according to claim 1 or 2,
Said fuel gas being directed onto the outer surfaces of said pore burner and combusted with said metal (M)
Process for burning metal (M) using fuel gas. 4. The method according to any one of claims 1 to 3,
The combustion occurs at a temperature above the melting point of the salts formed in the reaction of the metal (M) and the fuel gas,
Process for burning metal (M) using fuel gas. 5. The method according to any one of claims 1 to 4,
Wherein the metal (M) is supplied as an alloy of at least two metals (M)
Process for burning metal (M) using fuel gas. 6. The method according to any one of claims 1 to 5,
After the combustion, the reaction products are separated,
Process for burning metal (M) using fuel gas. The method according to claim 6,
The separation is carried out with the aid of a cyclone,
Process for burning metal (M) using fuel gas. 8. The method according to any one of claims 1 to 7,
The reaction products of the combustion preferably comprise at least one expander turbine and / or at least one gas turbine and / or at least one heat exchanger and / or at least one boiler Used to generate energy,
Process for burning metal (M) using fuel gas. As an apparatus for the combustion of the metal (M)
The metal (M) is selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / or mixtures thereof,
The apparatus comprises:
A pore burner including a porous tube as a burner,
A feed unit for the metal (M), preferably in the form of a liquid, into the interior of the pore burner, which feeds a metal (M), preferably in the form of a liquid, feed,
A feed unit for fuel gas, designed to supply fuel gas, and
Optionally a heating device for providing said metal (M) in liquid form,
The heating device is designed to liquefy the metal (M)
Apparatus for combustion of metal (M). 10. The method of claim 9,
Wherein the feed unit for the fuel gas is arranged such that a feed unit for the fuel gas at least partially directs the fuel gas to the surface of the pore burner,
Apparatus for combustion of metal (M). 11. The method according to claim 9 or 10,
The pore burner is arranged such that the reaction products formed from the combustion and optionally the metal (M) can be removed by gravity from the surface of the pore burner,
Apparatus for combustion of metal (M). 12. The method according to any one of claims 9 to 11,
The pore burner is a group of iron, chromium, nickel, niobium, tantalum, molybdenum, tungsten, zirconium and alloys of these metals and also of steels such as stainless steel and chromium- , ≪ / RTI >
Apparatus for combustion of metal (M). 13. The method according to any one of claims 9 to 12,
Further comprising a separation unit for products of combustion of said metal (M), said separation unit being designed to separate combustion products of said fuel (M) and said fuel gas, said separation unit being preferably a cyclone reactor cyclone reactor,
Apparatus for combustion of metal (M). 14. The method according to any one of claims 9 to 13,
Further comprising at least one inflator turbine and / or at least one gas turbine and / or at least one heat exchanger and / or at least one boiler,
Apparatus for combustion of metal (M). The use of a pore burner comprising a porous tube as a burner for combustion of a metal (M) selected from alkali metals, alkaline earth metals, aluminum and zinc, and alloys and / or mixtures thereof with fuel gas.

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