KR900004525B1 - How to generate heat energy - Google Patents

Abstract

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Description

How to generate heat energy

1 is a flow explanatory diagram of a basic operation method of the method of the present invention.

2 is a flow explanatory diagram of an operation method with additional steps.

3 is a flow explanatory diagram of a deformation operation method.

4 is a flow explanatory diagram of another modified operation method.

5 is a flow explanatory diagram of another modified operation method.

6 is a flow explanatory diagram of another variant operation with additional reaction steps for product production.

7 is a flow diagram of an operation method in which methane is used as the primary fuel.

FIG. 8 is a flow explanatory diagram of an operation method similar to that shown in FIG. 7 in which syngas is combusted by air; FIG.

9 is a flow diagram of an operating method in which methane and hydrogen are used as primary fuels.

10 is also a flow explanatory diagram of another operation method.

11 is a flow diagram of an operating mode in which methane is treated without a catalytic reaction step.

The present invention relates to a method of generating thermal energy from a hydrocarbon fuel using an oxidation reaction, commonly referred to as combustion.

Water vapor (hereinafter referred to as "steam" for brevity) is the secondary energy carrier most widely used and required in relatively large quantities for the purpose of conversion to electrical energy and also for the purpose of heat generation. Such vapors are mainly produced in the oxidation reactions (called combustion) of oxygen (usually in the form of air) and fossil fuels, and thus, for heating purposes, for example for heating large complexes such as administrative buildings and private homes. By heating the apparatus and the power plant.

In the normal combustion of fossil fuels, the carbon contained in the fossil fuels is oxidized by oxygen in the air to form CO ₂ and CO, and the obtained carbon oxide gas, also referred to as flue gas, is usually simply released into the atmosphere. . However, this means that beneficial raw carbon is lost in connection with the further generation of energy. In addition, depending on the nature of the fossil fuel used, the combustion of the fossil fuel produces significant by-products such as sulfur compounds, nitrogen oxides, and lead that are released into the atmosphere. The amount of carbon reserves on the planet is limited and the fact that carbon is actually disposed of by the way the carbon oxide waste gas is currently treated is a problem, and the fact that the above-mentioned substances are released into the atmosphere is not a matter of our environment. That means there is a risk that it will be totally devastated in the near future.

In addition, the heating device should be located as close to the consumption area as possible to prevent loss of the system due to long distance transport. However, although it is predicted that the energy generation process performed in such a heating device does not produce any waste products which cause environmental pollution, so far this problem has not been satisfactorily solved.

According to the present invention, in a cyclic process consisting of a combustion reaction step and a cracking reaction step in series, an initial hydrocarbon having a reducing action as a primary fuel and carbon oxide gas from the combustion reaction step are introduced into the cracking reaction step to react with the synthesis gas. And the synthesis gas is passed as a secondary fuel from the cracking reaction stage to the combustion reaction stage in which the oxidant is supplied to oxidatively burn, thereby obtaining thermal energy in the form of steam, and burning the carbon oxide gas produced in the combustion reaction stage in the combustion reaction. A method is provided for generating thermal energy from a hydrocarbon fuel using an oxidative combustion reaction, which consists of taking from the stage and passing it through a cracking reaction stage with fresh primary fuel.

As can be seen in detail below, the method of the present invention enables a highly economical operation. Carbonaceous combustion products are recycled in such a way as to be fully used as reusable secondary fuels and / or chemical raw materials. Thus, the method of the present invention enables complete carbon recirculation, avoids the release of flue gas into the atmosphere, and also avoids any waste products that may cause air pollution, so that the method of the present invention operates in the immediate vicinity of residential areas. And thus can be operated in an inexpensive manner near the consuming area for thermal energy generation purposes.

The initial fuel (hereinafter referred to as primary fuel) used in the method of the present invention may be a known hydrocarbon compound having a reducing action and a mixture thereof. Thus, for example, the primary fuel used consists of petroleum products such as methane containing natural hydrocarbons, natural gas, coal gas, cracked gas, syngas, city gas, coke throw gas, naphthene, and waste gas from chemical processes. You can. Preference is given to using methane. If desired, other gases or gas mixtures to be used may first be subjected to a methanation process, where the methanation product is used as primary fuel in the process of the invention.

Primary fuel is preferably used in gaseous form in the process of the invention. When using high molecular hydrocarbons such as paraffin or mineral oil, olefins or naphthenes, it is advantageous to inject such substances in gaseous form before use in the present invention.

Initial materials may also include any solid fossil fuels such as, for example, lignite, coal mines, and the like. In this case, however, the material used must be treated by one known gasification reaction (reaction to form methanol) to impart a reducing action to the gaseous hydrocarbons.

In the cracking reaction stage of the process of the invention, the primary fuel reacts with the carbon oxide gas from the combustion reaction stage of the process to provide syngas. As long as CO ₂ is produced in this operation, it is removed from the gas mixture and recycled to the cracking reaction stage or, if necessary, added to the catalytic reaction stage disposed downstream of the combustion and cracking reaction stage.

In the cracking reaction step, methane and carbon dioxide produce large amounts of carbon monoxide and hydrogen which are decomposed. The primary fuel and carbon oxide may be thermally reacted in the cracking reaction, and the reduction operation is carried out by endothermic or autothermal or preferably catalysis. When using a catalysis mode, it is advantageous to use nickel-containing or magnesium-containing catalysts. The following reactions can occur in this operation.

The manner of operation in the cracking reaction step and the composition of the syngas generated therein can be adjusted to a range of variables.

Thus, for example, the composition of the carbon oxides or carbon containing gases used with the primary fuel can be varied by the oxidant to be added to the combustion reaction step. When pure oxygen gas is conveniently used as the oxidant in the combustion reaction step, the waste gas generated from the combustion reaction step is carbon oxide gas containing no nitrogen. Although the gas contains a certain amount of water vapor, it does not interfere in the cracking reaction step as shown by the chemical equation.

In this case, the waste gas from the combustion reaction stage can thus be introduced in the cracking stage without further treatment such as cooling or cleaning. However, it will be appreciated from the energy point of view that the gas from the combustion reaction step is subjected to a cooling operation first. In this case the water component contained therein is completely or substantially removed in the cooling step. This gives the advantage that the primary fuel can be advantageously preheated by using it as a coolant for the waste gas before it is introduced into the cracking reaction stage. The water removed from the waste gas in the cooling stage is passed to a water reservoir which receives the heat liberated in the combustion reaction stage, for example in the form of steam such as a heat carrier.

The ratio of CO: H ₂ of the synthesis gas formed in the cracking reaction step may be changed. This ratio is matched to the oxygen-containing carbon product to be produced in subsequent catalytic catalytic reaction steps. For example, if an alcohol such as methanol is to be produced in the catalytic reaction step as an oxygen-containing carbon product (hereinafter referred to as secondary fuel), the syngas from the cracking reaction step is about 1: 2, preferably 1: 2.2 of CO: H _2. It is preferred to be adjusted to provide. If, for example, the isobutyl oil compound is to be produced in the catalytic reaction step to provide secondary fuel, the cracking reaction step is carried out in a manner to provide a syngas having a high CO content.

In order to control the CO: H ₂ ratio, hydrogen may be additionally introduced into the cracking reaction step. It may also be manipulated with water vapor in the cracking reaction step to avoid the formation of soot.

If the syngas leaves the cracking reaction step at high temperature, it may be passed through a relief or expansion means before feeding to the catalytic reaction step to take advantage of the remaining enthalpy.

The properties of the secondary fuel produced in the catalytic reaction stage are measured from one point to another depending on the requirements for the chemical raw material as the product. Part of the secondary fuel in the process according to the invention is preferably removed from the circulating process for use directly as a chemical raw material constituting the product, and only the remainder of the secondary fuel is introduced from the catalytic reaction stage into the combustion reaction stage. The amount of two-dimensional material obtained as a product from the circulation process of the present invention and used directly as a chemical raw material is advantageously made to correspond approximately to the amount of primary fuel newly supplied to the process in the cracking reaction step. This gives the advantage that the amount of carbon compound included in the circulation process remains substantially the same. The amount of carbon in the circulation process remains constant.

According to the present invention, only a part of the synthesis gas from the cracking reaction step can be supplied to the catalytic reaction step, and the remaining part can be passed directly to the combustion reaction step. It is also possible to selectively allow a portion of the syngas from the cracking reaction stage to be passed to the catalytic reaction stage and the remaining portions to separate reaction stages arranged in parallel relationship. This is desirable when the raw material is to be obtained as a by-product.

In addition, the syngas obtained from the cracking reaction step may be reacted with a substance removed at another point in the circulation process. One that may be mentioned in this regard is the oxygen-containing carbon compound removed from the catalytic reaction step. The oxygen-containing carbon compound may also be reacted with carbon monoxide obtained from syngas. This can lead to the production of chemical raw materials that are very important to the chemical industry, such as acetaldehyde and ethanol, as by-products of the process of the present invention, based on the following theoretical reactions.

Synthesis gas is preferably exothermic in the presence of an equivalent catalyst in the catalytic reaction step. In this case, the reaction theoretically occurs as follows.

When the syngas obtained from the cracking reaction step has a ratio of CO: H ₂ higher than 1: 2, it is preferable that hydrogen is additionally supplied to the catalytic reaction step. If the presence of CH ₄ is necessary to avoid the formation of waxes and the formation of polymeric hydrocarbons, CH ₄ can be further passed through the catalytic reaction stage to diverge from the suction conduit for the primary fuel. The next reactor is the reactor that actually occurs.

Parallel reactions for the formation of methanol depend on the stoichiometric ratio.

The ratio is measured relative to the CH ₄ / CO ₂ ratio at the inlet of the cracking reaction step.

In the case of exothermic reaction, the heat dissipated in the catalytic reaction step is advantageously recovered by using steam as the heat carrier and used in a desired manner. In the combustion reaction stage, the secondary fuel is combusted by the supplied oxidant (preferably pure oxygen or air). The thermal energy obtained in this reaction is delivered to energy consumers who use water vapor as the heat carrier. In the cooled or uncooled state, the waste gas is recycled with the new primary fuel to the cracking reaction stage and reused in the manner described above.

If air is used as the oxidant in the combustion reaction step, it is desirable to separate the carbon free components from the waste gas before the waste gas is combined with the new primary fuel. Nitrogen separated in this way can be released into the atmosphere. If this is done, there is no loss of fuel material and the atmosphere is not polluted. Nitrogen released in this way is in fact the only waste product from the circulation process of the present invention.

These nitrogens appear in relatively pure form for use in useful purposes. For example, it may be used as a coolant or an inert gas, depending on the economic point of view.

The operation of separating the carbon-containing component and the carbon-free component from the waste gas from the combustion reaction step is advantageously performed in the gas decomposition or separation step disposed downstream of the combustion reaction step. The waste gas can be separated in the separation step by, for example, a process involving pressure and temperature, a liquid washing process, a process and pressure process involving pressure and temperature, a semipermeable membrane, or a foreign matter gas dispersion process. .

Referring to the present invention in more detail based on the accompanying drawings as follows.

In all embodiments, the primary fuel used is CH _{4, which} is introduced into the circulation process through conduit 2.

In FIG. 1, the primary fuel passes through the cracking reaction step 17 through the conduit 2, while carbon oxide or carbon containing gas passes through the cracking reaction step 17 through the conduit 3. The carbonaceous gas exits the combustion reaction step 11 via the conduit 9. In the cracking reaction step 17, the primary fuel and carbon oxide gas are decomposed to form carbon monoxide and hydrogen. The syngas formed in this reaction passes through a catalytic reaction step 18 through a conduit 4 where it is converted to secondary fuel CH ₃ OH. The reaction is exothermic. The heat generated in this reaction can be recovered isothermally to the boiling water, and the thermal energy can be used as steam.

Syngas exits from reaction step 17 with a high proportion of steam, called a CO ₂ -cycle gas. The temperature is 860 ° C. while the pressure is 15 bar. A high energy content gas-vapor mixture is used for this purpose, which in the reaction step 17 is passed to a waste heat boiler in which the amount of steam required for the cracking process is produced to form a primary reformer. The gas-vapor mixture leaves the waste heat system at a temperature of about 250 ° C. and a pressure of 14.5 bar, and thus still has a high level of energy used. The gas-vapor mixture is passed to an inflatable turbine that drives the compressor. The compressor was fed through (1) syngas from a CO ₂ wash operation for subsequent methanol synthesis, (2) CO ₂ cycle gas, and (3) conduits (2 and 3) to decompose (CH ₄ + CO ₂ ). Compress the gas to be made.

The discharge temperature of the gas-vapor mixture depends on the total compression force of the device. In general, the energy of the gas-vapor mixture may be used upon inhalation of the inflatable turbine until condensation occurs on the water vapor components contained in the gas-vapor mixture. In this case the drive turbine is called a condensation turbine, and if only a small amount of energy is required due to the quantitative proportion of the gas to be compressed, the excess energy can be used for further steam generation in the waste heat system.

Secondary fuel (CH ₃ OH) is sent through a conduit (6) to the boiler for the combustion reaction step (11) and combusted by an oxidant applied through the conduit (7). The heat energy dissipated in this operation is recovered by the water supplied through the conduit 8 and water vapor as a heat carrier and can be used for other applications as required.

In FIG. 2, air is introduced into the combustion reaction step 11 through conduit 7 and acts as an oxidant. The waste gas removed through the conduit 9 is first precooled in the cooler 12. The coolant used is the primary fuel introduced through conduit 2. The primary fuel passes to the reaction stage 17 where it is preheated to form the cracking reaction stage in the preheated state. The waste gas is cooled in the cooler 12 and then passes through the conduit 9a to be compressed in the compressor 13 and from there through the conduit 9b to the column 14.

In column 14, the carbonaceous gas component is separated from the nitrogen gas component. Nitrogen is extracted at the top of column 14 through conduit 10a and expanded in expansion means 16, such as an inflatable turbine. Nitrogen may then be released into the atmosphere through conduit 10 or may be removed in other ways for other uses.

Carbon oxide gas containing no nitrogen passes from column 14 to evaporator 15 via conduit 9c. From the evaporator 15, the gas passes through the conduit 3 to the reaction stage 17. Syngas formed in the cracking reaction stage of the reactor 17 passes through the conduit 4 to the catalytic reaction stage 18. Some of the methanol formed here is removed via conduit 5 as product methanol, as a chemical raw material for a separate reaction. Some of the methanol formed in the catalytic reaction stage 18 passes through the conduit 6 as a secondary fuel to the combustion reaction stage of the boiler 11 and is burned there. When combustion occurs, the generated combustion energy is removed again with the water vapor supplied through the conduit 8 as a heat carrier for the purpose for which it is intended. If desired, the product methanol, which is removed from the catalytic reaction stage 18 through the conduit 5 and which has a constant heat content as a result of the exothermic reaction in the catalytic reaction stage 18, is circulated for use in other ways as a chemical raw material. It may be used as a heating agent for the expansion step in the evaporator 15 prior to removal from the furnace.

The embodiment shown in FIG. 3 is a modification of the method shown in FIG. The waste gas removed from the combustion reaction body 11 through the conduit 9 is first passed to the cooler 12 and subjected to precooling before passing the cracking reaction step in the reactor 17 through the conduit 3. In the cooler 12 the coolant is the primary fuel, which is introduced into the circulation process through the conduit 2 and also passed to the reactor 17 when preheated in this manner. Water contained in the waste gas separated in the cooling operation is removed from the cooler 12 through the conduit 29. This water may be applied to the water passing through the combustion reaction boiler 11 to the conduit 8 as a heat carrier. Some manner of operation of the method between the cracking reaction step 17, the catalytic reaction step 18 and the combustion reaction step 11 is as described above with reference to FIG. 2 in the embodiment of FIG. 3. The difference is that the oxidant introduced into the combustion reaction stage 11 through the conduit 7 is produced from the air introduced into the air separator 26 through the conduit 27 in the air separator 26 disposed upstream. Being pure oxygen is the point. In this case also nitrogen is the only waste product produced separately from the condensate from the cooler 12. In this mode of operation nitrogen may be removed through conduit 28 of device 26 to be treated or used in the manner described above with respect to FIG.

4 shows another embodiment, the operation of the combustion reaction step 11, the treatment of the waste gas from the combustion reaction step 11, and the charging of the cracking reaction step 17 are described with reference to FIG. As The difference is that the syngas removed from the cracking reaction step 17 through the conduit 4 is split before passing to the catalytic reaction step 18.

Some are passed through a conduit 4a to the catalytic reaction stage and converted to the oxygen-containing carbon compound CH ₃ OH obtained as product methanol via the conduit 5 as described.

The other part of the syngas is introduced into the direct combustion reaction step 11 as secondary fuel and combusted through the conduit 4b. Energy is obtained by the heat carrier through the conduit 8.

The embodiment shown in FIG. 5 is similar to the operating manner of the method as described in connection with FIG. In the method of FIG. 5, however, there are two coolers 12a and 12b between the gas separation stage and the combustion reaction stage 11, which consist of the compressor 13, the column 14 and the expansion means 15 and 16. The waste gas is precooled in the cooler 12a, where the coolant used is passed through the conduit 7 and then to the conduit 6 to which secondary fuel is supplied. Thus in this case the mixing of oxidant (air) and secondary fuel already takes place before the gas passes into the combustion reaction step (11). This has a beneficial effect on the efficiency of the combustion reaction.

After precooling in the first cooler 12a, the waste gas passes through the conduit 9d to the second cooler 12b. In the second cooler 12b, the waste gas is cooled by a coolant composed of primary fuel supplied through the conduit 2.

Thereafter, the operation manner for further treating the waste gas is as described with reference to FIG. Condensate is removed from cooler 12b via conduit 29, a portion of which is removed from the circulation process at 30. This is achieved in part via conduit 31, where water passes from conduit 31 to conduit 8 and acts as a heat carrier to receive energy.

In FIG. 6, the solid line shows the operation method as shown in FIG. The dashed line is a modified operation to obtain additional products suitable for use as chemical raw materials. In the embodiment of FIG. 6, only a portion of the syngas formed in the reaction step 17 passes through the conduit 4 into the catalytic reaction step 18. The other portion of the syngas passes through conduit 23 to the reactors 21 connected in parallel. In the reactor 21, the syngas reacts according to the following reaction formula.

CO is removed from reactor 21 and passes through conduit 24 to another reactor 19. Methane is branched from conduit 2 and then fed to reactor 19 through conduit 2a. Acetaldehyde is produced in reactor 19 according to the following scheme.

Acetaldehyde is reduced to ethanol by hydrogen introduced via feed conduit 32 according to the following equation through a conduit 25 to another reaction stage formed by the catalytic reactor indicated by reference numeral 20. .

Dialcohol is removed as product ethanol through conduit 22. CH ₃ OH formed in reactor 21 is removed therefrom and passes through conduit 6 via conduit 6a as additional secondary fuel. In this way, it passes to the combustion reaction step 11 with the secondary fuel resulting from the catalytic reaction step 18. The method of this embodiment provides product methanol and product ethanol in addition to thermal energy removed via conduit 8 and nitrogen removed from conduits 10 and 28 and water removed via conduits 29 and 30. Product methanol is removed via conduit 5 and product ethanol is removed via conduit 22. Acetaldehyde is also optionally removed from the reactor 19 as a reusable product.

7 shows a special embodiment, in which methane constitutes a primary fuel which is introduced into a mild process and mixed in a mixer with carbon oxide gas resulting from the combustion reaction step carried out in the boiler 11. The mixture is compressed in a compressor to react in the cracking reaction step to form syngas. Syngas has a high proportion coming out of the cracking reaction stage with water vapor, which is called a CO ₂ cycle gas.

The temperature is 860 ° C. at a pressure of 15 bar. The high energy content of this gas-steam mixture is first used by the mixture passing through the waste heat boiler to produce the amount of steam (primary modifier) required for the cracking process in the reactor 17. The gas-vapor mixture leaves the waste heat system at a temperature of about 250 ° C. and a pressure of 14.5 bar, and thus still has a high energy level. It is used by a vapor-gas mixture which is passed to an inflatable turbine which acts as a compressor driving means of this energy. The compressor performs the following operation.

1. Compression of syngas from the CO ₂ washing operation for continuous methanol synthesis, 2. Compression of CO ₂ cycle gas, and 3. Gas to be decomposed through conduits (2 and 3) (CH ₄ + CO ₂₎ ) Compression.

The discharge temperature of the gas-vapor compound depends on the overall compressor capacity of the unit. In general, the energy of the gas-vapor mixture at the turbine inlet can be used until condensation of the water vapor components contained in the gas-vapor mixture occurs.

In this case, the drive turbine is called a condensation turbine. Due to the quantitative proportion of the gas to be compressed, when only a small amount of energy is needed, the extra energy can be used for further steam generation in the waste heat system. Some of the compressed syngas is sent to the methanol synthesis process at the catalytic reaction stage and the other is combusted in the boiler (11). It is produced by an oxygen apparatus disposed upstream of the boiler 11 and combusted by pure oxygen mixed with syngas before passing to the boiler. Nitrogen is removed from the oxygen system for the desired use. Methanol produced in the methanol synthesis step is removed from the process in the form of highly useful products.

FIG. 8 is an embodiment of a method of operation of the method comprising operating in the manner shown in FIG. However, syngas is burned by air. In this way, not only the waste gas from the boiler 11 is cooled but also passes through a first CO ₂ washing step in which nitrogen from the combustion air is removed from the gas. The first CO ₂ washing operation, as described above, the carbon oxide or carbon containing gas is mixed with the primary fuel, ie methane, and the mixture is compressed. The compressed mixture is subjected to decomposition and the resulting synthesis gas-vapor mixture passes through a waste heat system and a second CO ₂ washing step. The compressed syngas passes in part to the methanol synthesis process and in part to the combustion reaction process in the boiler 11 with the addition of air. In this example, the CO ₂ cycle gas is washed twice.

FIG. 9 is an embodiment of the method as shown in FIG. 7, wherein the primary fuels used are methane and hydrogen. This embodiment has the advantage that much less methane is required due to the addition of hydrogen. The other steps in this method are largely the same as in FIG.

FIG. 10 is an embodiment of a method modified in a different manner compared to the method shown in FIG. Methane is also the primary fuel introduced into the cycle. At the same time, however, about 50% by volume of waste gas from the combustion reaction stage is released into the atmosphere downstream of the cooler. In this type of method, the amount of methane and steam required is different from the embodiment described above with respect to FIG.

11 shows an example of a circulation process, which is carried out without a catalytic reaction step. Methane is also used as the primary fuel. As described in connection with FIG. 7, it is mixed with the cooled carbon oxide gas resulting from the combustion reaction step.

The mixture is compressed and then the compressed mixture is reacted in the cracking reaction step to form syngas. The energy content of the syngas-vapor mixture attached to the cracking reaction stage is used as described above. After being extruded from the compressor through a CO ₂ washing step, the syngas is mixed with the oxygen produced by the oxygen system and passed through the boiler to produce combustion and heat therein. This example is operated without the production of methane.

Thus, as can be seen from the foregoing, the present invention provides a method for generating steam, heat and power as heat carriers in such a way that substantially no loss of carbon and no harmful substances are released into the atmosphere.

Claims (29)

A method of generating thermal energy from a hydrocarbon fuel using an oxidative combustion reaction, comprising: a circulating process consisting of a combustion reaction step and a cracking reaction step in series, from an initial hydrocarbon and combustion reaction step having a reducing action as a primary fuel Carbon oxide gas is introduced into the cracking reaction step to react to form a synthesis gas, and the synthesis gas is passed as a secondary fuel from the cracking reaction step to a combustion reaction step in which an oxidant is supplied to oxidatively burn and thermal energy in the form of steam. And carbon dioxide gas produced in the combustion reaction stage is taken from the combustion reaction stage and passed along with the new primary fuel to the cracking reaction stage. The method of claim 1, wherein the catalytic reaction step is interposed between the cracking reaction step and the combustion reaction step, at least a portion of the synthesis gas from the cracking reaction step is passed through the catalytic reaction step to contact the reaction to form an oxygen-containing carbon compound secondary A method of generating thermal energy characterized in that it is selectively passed through a combustion reaction step as fuel to combust to generate heat, or removed as a product for a separate use. 3. The method of claim 2 wherein a portion of the syngas from the cracking reaction stage is passed through a catalytic reaction stage and the other portion is passed through a combustion reaction stage. 3. The thermal energy of claim 2, wherein a portion of the syngas from the cracking reaction stage is passed through a catalytic reaction stage and another portion of the syngas from the cracking reaction stage is passed through other reaction stages connected in parallel. How to raise. The method of claim 1, wherein the primary fuel is introduced into the cracking reaction step in gaseous form. The method of claim 1, wherein the primary fuel and the carbon oxide gas are thermally reacted in a cracking reaction step. The method of claim 1, wherein the primary fuel and the carbon oxide gas are catalytically reacted in a cracking reaction step. 8. The method of claim 7, wherein a nickel containing catalyst is used. 8. The method of claim 7, wherein a magnesium containing catalyst is used. The method of claim 1, wherein the syngas is exothermic at a catalytic reaction stage in the presence of a copper-containing catalyst. 12. The method of claim 10, wherein the removal of heat from the catalysis step is performed isothermally with respect to water and energy is obtained from the formed vapor. The method of claim 1 wherein oxygen (O ₂ ) is used as the oxidant in the combustion reaction step. 13. The method of claim 12, wherein oxygen from the air separation process is used as the oxidant in the combustion reaction step. The process according to claim 1, wherein air is used as an oxidant in the combustion reaction step, and a gas separation step is disposed downstream of the combustion reaction step to separate the waste gas from the combustion reaction step into a carbon-containing component and a carbon-free component, A method of generating thermal energy characterized by removing a carbon-free component from the circulation process. 15. The method of claim 14, wherein the waste gas from the combustion reaction stage is separated in a gas separation stage by a pressure-temperature process. 15. The method of claim 14, wherein in the gas separation step, the carbon-containing component is separated by a wash liquid. 15. The method of claim 14, wherein the waste gas from the combustion reaction stage is separated in the gas separation stage by mixing pressure-temperature and washing process. 15. The method of claim 14, wherein the carbon-free component is separated by a semipermeable membrane. 15. The method of claim 14, wherein the waste gas from the combustion reaction stage is separated in a gas separation stage by a foreign matter gas dispersion process. 2. The method of claim 1, wherein the waste gas from the combustion reaction stage is cooled in a cooling stage using the primary fuel as a coolant, while simultaneously preheating the primary fuel. The method of claim 1 wherein methane is used as the primary fuel. 2. The method of claim 1, wherein natural gas is used as the primary fuel. 22. The method of claim 21, comprising a catalytic reaction step carried out in the form of a methanol synthesis process, wherein the methanol formed in the catalytic reaction step is removed from a mild process for a separate use to generate thermal energy, characterized in that obtained in the form of a product How to let. The method of claim 1, wherein the primary fuel is composed of at least one polymer hydrocarbon, such as paraffin or mineral oil, but formed into a gaseous state prior to introduction into the cracking reaction step. The method of claim 1, wherein the primary fuel is composed of at least one olefin but formed into a gaseous state prior to introduction into the cracking reaction step. The method of claim 1, wherein the primary fuel is composed of at least one naphthene but formed into a gaseous state prior to introduction into the cracking reaction step. The method of claim 1 wherein waste heat of the waste gas from the combustion reaction stage is used to preheat the primary fuel and / or oxidant to be introduced into the combustion reaction stage. The method of claim 1, wherein hydrogen is further introduced into the cracking reaction step. The method of claim 1, wherein hydrogen is further introduced into the catalytic reaction step.

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