Method for production of synthesis gas (options)

 

The invention relates to a method of manufacturing a synthesis gas, intended for use in the synthesis of gasoline, methanol or dimethyl ether. Method for the production of synthesis gas, which runs the plant for the synthesis containing the reforming-installation, having the reaction tube for steam reforming, the radiation of the combustion chamber is created around the reaction tube, for heating the reaction tube and convection section, built with radiant combustion chamber. Natural gas containing steam is created by adding steam to natural gas. Natural gas containing steam, preheated by passage of gas through the convection section of the installation, and then pre-heated natural gas is introduced into the reaction tube. After pre-heating in the convection section of the carbon dioxide is introduced into the reaction tube, and the produced synthesis gas containing hydrogen and carbon monoxide. This invention allows to reduce the consumption of heat the reforming install and effectively use excess heat installation. 4 C. and 14 C.p. f-crystals, 5 Il.

The present invention relates to a method proizvodstva process GTL (gas-liquid).

Synthesis gas containing hydrogen (H2) and carbon monoxide (CO), used as starting material for the synthesis of gasoline and the like through a process of GTL (gas-liquid) according to the system of reactions of Fischer-Tropsch.

This synthesis gas is typically produced by the following method.

Namely, by using the installation for synthesis gas, is equipped with a reformer (reforming-install) containing the reaction tube for steam reforming, radiation combustion chamber located around the reaction tube, for heating the reaction tube by the combustion and convection section, built with radiant combustion chamber, steam and carbon dioxide is added to natural gas, is used as the source gas, to obtain a mixed gas, which then passes through the convection section to be heated to a predetermined temperature. Received a pre-heated mixed gas is then injected into the reaction tube for the steam reforming of natural gas, along with carbon dioxide, synthesis gas containing hydrogen (H2) and carbon monoxide (CO). Since the temperature of the reaction tube, which should nicoga mixed gas, this pre-heating could contribute to the reduction of fuel consumption.

A known method for production of synthesis gas by the passage of gas containing steam through heat exchange reformer, partial combustion deformirovannogo flow with obtaining the secondary flow passage of the secondary flow on the outside of the tubes of the heat exchange reformer to heat the gas inside the tubes and the cooling of the secondary stream, further cooling of the secondary flow, the allocation of a carbon dioxide and feeds it into heat-exchange reformer (WO 00/09441, publ. 24.02.2000).

However, if natural gas containing steam and carbon dioxide, pre-heated to a temperature of from 550 to 600oWith or more in the convection section of the reformer and in accordance with the conventional method, there is a thermal decomposition of hydrocarbons, starting With2(ethane) or more high molecular weight, natural gas, thereby forming carbon. So produced carbon tend to settle on the inner wall of the section for pre-heating natural gas (pipeline), thereby deteriorating characteristics of the heat pipe and, therefore, reducing the rate of heat transfer.

In addition, if the tempo is eve may be damaged.

In addition, if so produced, the carbon gets the access layer catalyst enclosed in a reaction tube of a reformer and located on the output side section of the preheating, the catalyst layer may be clogged, thereby adversely affecting the reaction and heat transfer, or in certain circumstances, as a catalyst, and the reaction tube may be damaged.

Therefore, to prevent unnecessary consumption of natural gas in the case of pre-heating natural gas containing steam and carbon dioxide, in the convection section of the reformer in a conventional method of manufacturing a synthesis gas required to maintain the temperature of pre-heating less than 560oS. according to the conventional method is difficult to reduce consumption of fuel reformer and effective implementation of the extraction of heat in the convection section.

Therefore, the present invention is to provide a method for the production of synthesis gas, which makes possible the introduction of natural gas containing steam and carbon dioxide and heated to a relatively high temperature in the reforming installation, the CA is the volumetric heat installation.

Namely, the present invention provides a method for the production of synthesis gas by the use of plants for the synthesis containing the reforming unit (reformer), with the reaction tube for the steam reforming process, the radiation of the combustion chamber is created around the reaction tube, for heating the reaction tube by the combustion of fuel, and a convection section, built with radiant combustion chamber, and the method comprises the stage of: adding steam to natural gas to produce natural gas containing steam; passing the natural gas containing steam, through the convection section of the reformer installation, thereby pre-heated natural gas, containing pairs; preheating the carbon dioxide by passing carbon dioxide through the convection section of the reformer installation; introducing preheated natural gas containing steam and preheated carbon dioxide in the reaction tube, you get a synthesis gas containing hydrogen and carbon monoxide.

The carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber of the reformer installation, or douchesmalay also a method for the production of synthesis gas by use of installation for synthesis, containing reforming-installation and pre-reforming-setting, which provides before you install during the process, the reforming plant includes a reaction tube for steam reforming, the radiation of the combustion chamber is created around the reaction tube, for heating the reaction tube by the combustion of fuel, and a convection section, built with radiant combustion chamber, the method comprises the stage of: adding steam to natural gas to produce natural gas containing steam; passing the natural gas containing steam, through the convection section of the reformer installation, thereby preheat the natural gas containing steam; the introduction of preheated using a pre-reforming-installation of natural gas containing steam, into the reaction tube; preheating the carbon dioxide by passing carbon dioxide through the convection section of the reformer installation; introduction carbon dioxide is preheated in the passage, which is located between the reaction tube and the pre-reforming-install, and passing the preheated natural gas containing steam in the reaction tube, while p is its gas, formed by the combustion products generated by radiation in the combustion chamber of the reformer installation, or carbon dioxide is removed from the synthesis gas produced by the reforming-installation.

The present invention also provides a method of producing synthesis gas by the use of plants for the synthesis containing the reforming installation and furnace for partial oxidation, which provides for reforming the installation during the process, while the reforming system includes a reaction tube for steam reforming, the radiation of the combustion chamber is created around the reaction tube, for heating the reaction tube by burning fuel, and a convection section, built with radiant combustion chamber, the method comprises the following stages:
adding steam to natural gas to produce natural gas containing steam;
the passage of the natural gas containing steam, through the convection section of the reformer installation, thereby preheat the natural gas containing steam;
preheating the carbon dioxide by passing carbon dioxide through the convection section of the reformer installation;
the introduction of preheated nature is given synthesis gas, containing hydrogen and carbon monoxide;
introducing the synthesis gas into the furnace for partial oxidation;
the introduction of a gas containing oxygen into the furnace for partial oxidation, thus conducting the reaction between the synthesis gas and oxygen.

While carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber (12) reforming units, or carbon dioxide is removed from the synthesis gas produced by the reforming of installation. The gas containing oxygen, a represents oxygen or a mixed gas containing oxygen and carbon dioxide. Steam is additionally injected into the furnace for partial oxidation.

The present invention also provides a method of producing synthesis gas by the use of plants for the synthesis containing the reforming-setting, pre-reforming-setting, which is placed before the reforming installation during the process, and the furnace for partial oxidation, which provides for the installation, and reforming the installation process includes the reaction tube for steam reforming, the radiation of the combustion chamber is created around the reaction tube, d is a measure of combustion, the method comprises the following stages;
adding steam to natural gas to produce natural gas containing steam;
the passage of the natural gas containing steam, through the convection section of the reformer installation for preheating the natural gas containing steam;
the introduction of preheated using pre-reforming-installation of natural gas containing steam, into the reaction tube;
preheating the carbon dioxide by passing carbon dioxide through the convection section of the reformer installation;
introduction carbon dioxide is preheated in the passage, which is located between the reaction tube and the pre-reforming-install, and passing the preheated natural gas containing steam in the reaction tube, you get a synthesis gas containing hydrogen and carbon monoxide;
introducing the synthesis gas into the furnace for partial oxidation;
the introduction of a gas containing oxygen into the furnace for partial oxidation, thereby making the reaction between the synthesis gas and oxygen.

While carbon dioxide is removed from flue gas formed by combustion products generated in the radiation charming installation. The gas containing oxygen, a represents oxygen or a mixed gas containing oxygen and carbon dioxide, and into the oven for partial oxidation impose additional pairs.

Additional objectives and advantages of the present invention will be presented in the following description and will partly be obvious from the description or can be learned in the implementation of the present invention. Objectives and advantages of the present invention may be realized and attained by means of the devices and their combinations specified below.

The accompanying drawings, which are attached and form part of the description, illustrate preferred at present, examples of embodiments of the present invention, and together with the General description given above and the detailed description of the preferred embodiments given below, serve to explain the principles of the present invention.

Fig. 1 is a block diagram illustrating the main stages of the production process of the synthesis gas in the synthesis of gasoline, kerosene and gas oil, which can be used according to the first embodiment of the present invention.

Fig. 2 is a block-scheme is arocena and gasoil, which can be used according to the second embodiment of the present invention.

Fig. 3 is a block diagram illustrating the main stages of the production process of the synthesis gas in the synthesis of gasoline, kerosene and gas oil, which can be used according to the third embodiment of the present invention.

Fig. 4 is a block diagram illustrating the main stages of the production process of the synthesis gas in the synthesis of gasoline, kerosene and gas oil, which can be used according to a fourth embodiment of the present invention;
Fig. 5 is a block diagram illustrating the main stages of the production process of the synthesis gas in the synthesis of gasoline, kerosene and gas oil, which can be used according to the fifth embodiment of the present invention.

Now the method of manufacturing a synthesis gas (which is suitable for use in the synthesis of gasoline, kerosene and gas oil) will be explained with reference to the drawings.

Fig. 1 is a block diagram illustrating the main part of the installation for synthesizing gasoline, kerosene and gas oil, which can be used in the production of synthesis is built to use steam reforming, radiation combustion chamber 12 located around the reaction tube 11 and is designed for heating the reaction tube by burning fuel, and the exhaust pipe 14, which is communicated through the convection section (section to extract excess heat) 13 radiation combustion chamber 12. The reaction tube 11 inside is filled with a catalyst, for example, Nickel-based. The passage 211for the introduction of fuel reported with radiation combustion chamber 12 of the reformer installation (reformer) 10.

The passage 202for introducing the source gas is communicated through the convection section 13 of the reformer 10 with the upper part of the reaction tube 11. This passage 202for the introduction of the source gas can be supplied desulfuration (not shown). The passage 203for the introduction of a pair communicates with the passage 202for the introduction of the source gas, which is located in the input part of the convection section 13. The passage 204for the introduction of carbon dioxide is located so that it passed through the convection section 13 near the radiation of the combustion chamber 12 of the reformer 10 (i.e. in the field of high temperatures inside the convection section 13), and then it was reported that part of the passage 202for uvedorei intersects the passage 202for the introduction of the source gas. Preferably the passage 204for the introduction of carbon dioxide is located so that it was reported that part of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11.

The lower part of the reaction tube 11 of the reformer 10 is communicated through passage 205device for separating gas and liquid 31. This passage 205provided with a heat exchanger 32. This heat exchanger 32 intersects with the passage 206thus, to heat, for example, boiling water passing through the passage 206, this will generate high pressure steam. The water separated by the device for separating gas and liquid 31, provide an opportunity to emerge from the reformer 10 through the passage 207. Gas (synthesis gas), selected using the device for separating gas and liquid 31, provide an opportunity to flow through the passage 208in the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, a catalyst based on cobalt. The catalyst, which must be filled in this reaction system 33 FT, may not be limited to the catalyst based on cobalt, but may be, for example, rolled the ionic sections 13 of the reformer 10, thereby making it possible to heat the exhaust gas formed by combustion products, in the convection section 13 of boiling water. In the exhaust gas formed by combustion products, is cooled, and at the same time the boiling water is heated, thus generating high-pressure steam.

Now the method of manufacturing a synthesis gas will be explained with reference to the above setting for the synthesis shown in Fig.1.

First of all the fuel for combustion is injected through the passage 201for the introduction of fuel radiation in the combustion chamber 12 of the reformer 10 so as to enable the fuel to burn together with the air, thus heating the inner space of the reaction tube 11 to a sufficiently high temperature (for example, 850-900oC). This heating of the reaction tube 11 is due to the fact that the reforming reaction in the reformer 10 is an endothermic reaction. The exhaust gas formed by combustion products containing carbon dioxide, generated in the radiation of the combustion chamber 12, provide the ability to flow through the convection section 13 in the exhaust pipe 14. When the exhaust gas formed productalso warmth discussed below with natural gas, containing steam, which passes through the passage 202for the introduction of the source gas, with carbon dioxide flowing through the passage 204for the introduction of carbon dioxide, as well as boiling water flowing through the passage 209while cooling the flue gas formed by combustion products. The exhaust gas formed by the combustion products, chilled so, then give the opportunity to go into the atmospheric air through an exhaust pipe 14.

Natural gas containing methane as a main component, is introduced into the passage 202for the introduction of the source gas. At this point, through the passage 203for the introduction of steam to natural gas at a predetermined ratio add pairs to obtain natural gas containing steam. For instance, they can be used in steam, which is generated during the heat exchange between the boiling water and the synthesis gas in the heat exchanger 32 (will be explained later), as well as steam, which is generated during the heat exchange between boiling water and flue gas formed by combustion products, in the convection section 13 of the reformer 10.

Natural gas containing steam, give the opportunity to enter the passage 202for the introduction of the source gas and heating (up to tempera is radnom gas, for example, heating to 400-550o(C) when the natural gas containing steam, passes through the convection section 13 of the reformer 10, and then the natural gas containing steam, the heated, is introduced into the reaction tube 11, which is heated to a sufficiently high temperature. Carbon dioxide gives the possibility of passing through the passage 204for the introduction of carbon dioxide, which is reported through the convection section 13 near the radiation of the combustion chamber 12 with a passage 202for the introduction of the source gas, as discussed above. As a result, the carbon dioxide is preheated to a temperature of from 550 to 650oC, which is higher than the temperature specified above for natural gas containing steam, at a time when the carbon dioxide passes through the convection section 13 of the reformer 10. Because it is pre-heated carbon dioxide is injected into the area of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11, so that mixed with the above natural gas containing steam in the reaction tube 11 may be natural gas, which is mixed with duoci is, kiuchumi as a main component is methane (CH4), steam and carbon dioxide, which is introduced into the reaction tube 11 of the reformer 10, and then is subjected to a process of steam reforming, where methane is mainly subjected to steam reforming in the presence of a catalyst inside the reaction tube 11, and the produced synthesis gas containing hydrogen, carbon monoxide and carbon dioxide at a molar ratio of H2/CO, which varies from 1 to 2.5 according to the following equations (1) and (2).

CH4+H2OCO+3H2(1)
CO+H2OCO2+H2(2)
In these equations (1) and (2) reaction of the reformer 4 mol of hydrogen and 1 mol of carbon dioxide can be obtained by reacting 1 mole of methane and 2 moles of steam. Real reaction system, however, can be obtained a composition which is close to chemical equilibrium compositions, which can be determined by the temperature and pressure at the outlet of the reaction tube.

It would be preferable in the case of adding steam and carbon dioxide to natural gas to maintain the methane content in PR is ω (H2O) fell within: CH4:H2O=1:1.5 to 1:3; while the molar ratio between methane (CH4) and carbon dioxide (CO2) fell within: CH4:CO2=1:1-1:3.

The synthesis gas thus obtained is introduced through a passage 205in the heat exchanger 32 to thereby heat the boiling water flowing through the passage 206to generate high-pressure steam. At this time, the synthesis gas is cooled and then introduced into a device for the separation of gas and liquid 31 in which the water is separated from the synthesis gas separated so the water is subsequently removed from the system through the passage 207. Thus obtained synthesis gas is then fed through the passageway 208in the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, a catalyst based on cobalt, with the opportunity to hydrogen and carbon monoxide contained in the synthesis gas, to interact with each other, when this happens the synthesis of gasoline, kerosene and gasoil.

In accordance with this first example embodiment of the reformer 10 is constructed so that it contains the reaction tube 11, the radiation of the combustion chamber 12 for heating the reaction tube 11 through the introduction of natural gas, containing steam and carbon dioxide in the reaction tube 11 after pre-heating in the convection section 13 of the reformer 10 natural gas containing steam and carbon dioxide are introduced through separate passages respectively, i.e. natural gas containing steam, is injected through the passage 202for the introduction of the source gas, which is connected after passing through the convection section 13 of the reformer 10 with the reaction tube 11, while the carbon dioxide is injected through the passage 204for the introduction of carbon dioxide, which is connected after passing through a specific area of convection section 13 of the reformer 10 (specifically, through the region of high temperatures convection section 13, which is located near the radiation of the combustion chamber 12 with a passage 202for the introduction of the source gas, resulting in the flow of natural gas mixed with steam, and the flow of carbon dioxide are combined near the input device of the reaction tube 11. The result may be pre-heated carbon dioxide, which is inserted through the passage 204for the introduction of carbon dioxide in the convection section 13 in order to enable carbon dioxide to warm to the situations in natural gas, which can occur when natural gas is mixed with steam and carbon dioxide, are trying to be preheated in the convection section 13. Therefore, now is the possible introduction of natural gas mixed with steam and carbon dioxide in the reaction tube reformer under conditions when the natural gas is preheated to a high temperature, it is possible inhibition or prevention of the decomposition of hydrocarbons from C2or more high molecular weight in natural gas. In the result, since the amount of fuel that you must enter radiation in the combustion chamber 12 of the reformer 10 can be reduced, the interaction between natural gas (mainly methane in natural gas), steam and carbon dioxide can be efficiently carried out in the reaction tube using a minimum amount of fuel, and the produced synthesis gas containing CO and H2. Namely, the consumption of the fuel reformer can be reduced to a minimum.

In addition, since not only the passage 202for the introduction of the source gas, but also the passage 204for the introduction of carbon dioxide has the ability to pass through convection the camera 12) thus, to allow preheating of the carbon dioxide while passing carbon dioxide through the passage 204for the introduction of carbon dioxide, the excess heat from the reformer 10 can be effectively used.

This synthesis gas containing CO and H2may be introduced into the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, a catalyst based on cobalt, the hydrogen and carbon monoxide contained in the synthesis gas, are given the opportunity to interact with each other, thereby making possible the synthesis of gasoline, kerosene and gasoil.

Therefore, now it is possible to reduce the amount of fuel that you must enter radiation in the combustion chamber of the reformer, and the effective use of excess heat from the reformer for the production of synthesis gas containing CO and H2designed for synthesizing gasoline, kerosene and gas oil by, for example, the reaction system Fischer-Tropsch (FT), through the introduction of natural gas containing steam and carbon dioxide in the reformer.

Fig. 2 is a block diagram illustrating the main part of the installation for synthesizing gasoline, kerosene and gas oil, which mozek in the above Fig.1, are denoted by the same numbers in order to avoid their explanations.

This setting for the synthesis characterized by the fact that in the convection section 13 of the reformer 10 is a device for extracting carbon dioxide 34, thereby making possible the extraction of carbon dioxide from flue gas formed by combustion products from the convection section 13. This device for extracting carbon dioxide 34 is connected through the passage 2010with the compressor 35. This compressor 35 is communicated via passage 2011to introduce dioxide, which is located so that it passes through the convection section 13 near the radiation chamber 12 of the reformer 10 (i.e., high temperatures inside the convection section 13), with a part of the passage 202for the introduction of the source gas, which is located further along the process in relation to the convection section 13 and which intersects the passage 202for the introduction of the source gas. Preferably the passage 2011for the introduction of carbon dioxide is located so that it was reported that part of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11.

Now the way production is>/p>First of all the fuel for combustion is injected through the passage 201for the introduction of fuel radiation in the combustion chamber 12 of the reformer 10 so as to enable the fuel to burn together with the air, thus heating the inner space of the reaction tube 11 to a sufficiently high temperature (for example, 850-900oC). This heating of the reaction tube 11 is due to the fact that the reforming reaction in the reformer 10 is an endothermic reaction. The exhaust gas formed by combustion products containing carbon dioxide and generated in the radiation of the combustion chamber 12, provide the ability to flow through the convection section 13 in the exhaust pipe 14. When the exhaust gas formed by combustion products, passing through the convection section 13, the exhaust gas formed by combustion products, exchanges heat with discussed below natural gas containing steam, which passes through the passage 202for the introduction of the source gas, with carbon dioxide flowing through the passage 204for the introduction of carbon dioxide, as well as boiling water flowing through the passage 209while cooling the flue gas formed product is m thus, extracted using the device for extracting carbon dioxide, and then introduced through the passage 2010the compressor 35. The exhaust gas formed by the combustion products, which remove carbon dioxide, and then give the opportunity to go into the atmospheric air through an exhaust pipe 14.

Natural gas containing as a main component is methane, is introduced into the passage 202for the introduction of the source gas. At this point, through the passage 203for the introduction of steam to natural gas at a predetermined ratio add pairs to obtain natural gas containing steam. For instance, they can be used in steam, which is generated during the heat exchange between the boiling water and the synthesis gas in the heat exchanger 32 (will be explained later), as well as steam, which is generated during the heat exchange between boiling water and flue gas formed by combustion products, in the convection section 13 of the reformer 10.

Natural gas containing steam, allows you to enter in the passage 202for the introduction of the source gas and heated (to a temperature at which there can decompose the hydrocarbons2or more high-molecular compound existing in natural gas, for example, pre-heated to 400-55011for the introduction of carbon dioxide, which reported after passing through the convection section 13 near the radiation of the combustion chamber 12 with a passage 202for the introduction of the source gas as described above. As a result, the carbon dioxide is preheated to a temperature of from 550 to 650oC, which is higher than the temperature specified above for natural gas containing steam, at a time when the carbon dioxide passes through the convection section 13 of the reformer 10. Because it is pre-heated carbon dioxide is injected into the area of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11, so that mixed with the above natural gas containing steam, natural gas, which is mixed with carbon dioxide and steam and is heated to a higher temperature, can be introduced into the reaction tube 11.

The mixed gas, the content is that is introduced into the reaction tube 11 of the reformer 10, then undergoes a process of steam reforming, where methane is mainly subjected to steam reforming in the presence of a catalyst inside the reaction tube 11, and the produced synthesis gas containing hydrogen, carbon monoxide and carbon dioxide at a molar ratio of N2/CO, which varies from 1 to 2.5 according to the above equations (1) and (2).

It would be preferable in the case of adding steam and carbon dioxide to natural gas to maintain the methane content in natural gas, steam and carbon dioxide so that the molar ratio between methane (CH4) and steam (H2O) fell within: CH4:H2O=1:1.5 to 1:3; while the molar ratio between methane (CH4) and carbon dioxide (CO2) fell within: CH4:CO2=1:1-1:3.

The synthesis gas thus obtained is introduced through a passage 205in the heat exchanger 32 to thereby heat the boiling water flowing through the passage 206to generate high-pressure steam. At this time, the synthesis gas is cooled and then introduced into a device for the separation of gas and liquid 31 in which the water is separated from the synthesis gas separated so is then transported through the passage 208in the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, a catalyst based on cobalt, with the opportunity to hydrogen and carbon monoxide contained in the synthesis gas, to interact with each other, when this happens the synthesis of gasoline, kerosene and gasoil.

In accordance with this second embodiment is now possible in the same way as in the case of the first embodiment, to reduce the amount of fuel that you must enter radiation in the combustion chamber of the reformer, and effectively use the excess heat to the reformer for the production of synthesis gas containing CO and H2which is suitable for use in the synthesis of gasoline, kerosene and gas oil by, for example, the reaction system Fischer-Tropsch (FT), through the introduction of natural gas containing steam and carbon dioxide in the reformer.

In addition, since it is possible to produce carbon dioxide without the need for any other source of carbon dioxide because the carbon dioxide generated within production units (mainly in the reformer) to synthesis gas, which comprises the reaction system Fischer-Tropsch process can be extracted is mu gas, containing steam at the point of inlet of the reformer in order to be used as the source of gaseous material for ri-forming gas, synthesis gas containing hydrogen and carbon monoxide at a molar ratio of N2/CO, which is suitable for use in the synthesis of gasoline, kerosene and gas oil by the reaction system Fischer-Tropsch process can be cheaply produced in any place, not being limited by the location of a source of gaseous CO2such as an installation for producing ammonium. Moreover, it becomes possible to suppress the carbon dioxide, which, as expected, causes global warming, when it is separated from the production installation.

Fig. 3 is a block diagram illustrating the main part of the installation for synthesizing gasoline, kerosene and gas oil, which can be used in the production of synthesis gas according to the third embodiment. In Fig.3, the same components as in the above Fig.1, are denoted by the same numbers in order to avoid their explanations.

This installation for synthesis is characterized by the fact that the device for extracting carbon dioxide 36 is connected with a passage 205which is placed between tada 36 is connected through the passage 2012with the compressor 35. This compressor 35 is communicated via passage 2011to introduce dioxide, which is located so that it passes through the convection section 13 near the radiation of the combustion chamber 12 of the reformer 10 (i.e., through the region of high temperatures inside the convection section 13), with a part of the passage 202for the introduction of the source gas, which is located further along the process in relation to the convection section 13 and which intersects the passage 202for the introduction of the source gas. Preferably the passage 2011for the introduction of carbon dioxide is located so that it was reported that part of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11.

Now the method of manufacturing a synthesis gas will be explained with reference to the above setting for the synthesis shown in Fig.3.

First of all the fuel for combustion is injected through the passage 201for the introduction of fuel radiation in the combustion chamber 12 of the reformer 10 so as to enable the fuel to burn together with the air, thus heating the inner space of the reaction tube 11 to a sufficiently high temperature reforming in the reformer 10 is an endothermic reaction. The exhaust gas formed by combustion products containing carbon dioxide and generated in the radiation of the combustion chamber 12, provide the ability to flow through the convection section 13 in the exhaust pipe 14. When the exhaust gas formed by combustion products, passing through the convection section 13, the exhaust gas formed by combustion products, exchanges heat with discussed below natural gas containing steam, which passes through the passage 202for the introduction of the source gas, with carbon dioxide flowing through the passage 204for the introduction of carbon dioxide, as well as boiling water flowing through the passage 209while cooling the flue gas formed by combustion products. The exhaust gas formed by the combustion products, which remove carbon dioxide, and then give the opportunity to go into the atmospheric air through an exhaust pipe 14.

Natural gas containing as a main component is methane, is introduced into the passage 202for the introduction of the source gas. At this point, through the passage 203for the introduction of steam to natural gas add pairs at a given ratio to obtain natural gas containing steam. By the way, otnositelnogo and synthesis gas in the heat exchanger 32 (will be explained later), as well as steam, which is generated during the heat exchange between boiling water and flue gas formed by combustion products, in the convection section 13 of the reformer 10.

Natural gas containing steam, allows you to enter in the passage 202for the introduction of the source gas and pre-heated (to a temperature at which there can decompose hydrocarbons from C2or more high-molecular compound existing in natural gas, for example, pre-heated to 400-550o(C) when the natural gas containing steam, passes through the convection section 13 of the reformer 10, and then the natural gas containing steam, the heated, is introduced into the reaction tube 11, which is heated to a sufficiently high temperature. Carbon dioxide, which is removed from the synthesis gas by means of a device for extracting carbon dioxide 36 (to be explained below), are then introduced through the passage 2012the compressor 35 to increase the pressure therein. Carbon dioxide, the pressure of which is increased thus gets an opportunity together with carbon dioxide, which comes from the passage 2013to enter the passage 2011for the introduction of carbon dioxide, which is reported for the introduction of the source gas, as specified above. As a result, the carbon dioxide is preheated to a temperature of from 550 to 650oC, which is higher than the temperature specified above for natural gas containing steam, at a time when the carbon dioxide passes through the convection section 13 of the reformer 10. Because it is pre-heated carbon dioxide is injected into the area of the passage 202for the introduction of the source gas, which is located near the input device of the reaction tube 11, so that mixed with the above natural gas containing steam, natural gas, which is mixed with carbon dioxide and steam and is heated to a higher temperature, can be introduced into the reaction tube 11.

The mixed gas containing natural gas, comprising as a main component is methane (CH4), steam and carbon dioxide, which is introduced into the reaction tube 11 of the reformer 10, and then is subjected to a process of steam reforming, where methane is mainly subjected to steam reforming in the presence of a catalyst inside the reaction tube 11, and the produced synthesis gas containing hydrogen, carbon monoxide and carbon dioxide at a molar the lo would be preferable in the case of adding steam and carbon dioxide to natural gas to maintain the methane content in natural gas, steam and carbon dioxide so that the molar ratio between methane (CH4) and steam (H2O) fell within: CH4:H2O=1:1.5 to 1:3; while the molar ratio between methane (CH4) and carbon dioxide (CO2) fell within: CH4:CO2=1:1-1:3.

The synthesis gas thus obtained is introduced through a passage 205in the heat exchanger 32 to thereby heat the boiling water flowing through the passage 206to generate high-pressure steam. At this time, the synthesis gas is cooled and then introduced into the device for extracting carbon dioxide 36 from which to extract the carbon dioxide. Retrieved thus carbon dioxide is injected through the passage 2012the compressor 35. Carbon dioxide, in which the pressure is increased thus by using a compressor 35, is introduced together with natural gas containing steam in the reaction tube 11. Synthetic gas, from which the selected dioxide, to be entered in the device for separating gas and liquid 31 in which the water is separated from the synthesis gas that is allocated so the water is then removed from the system through the passage 207. Thus obtained synthesis gas then transport the torus on the basis of cobalt, the hydrogen and carbon monoxide contained in the synthesis gas, are given the opportunity to interact with each other, when this happens the synthesis of gasoline, kerosene and gasoil.

In accordance with this third embodiment is now possible in the same way as in the case of the first embodiment, to reduce the amount of fuel that you must enter radiation in the combustion chamber of the reformer, and effectively use the excess heat to the reformer for the production of synthesis gas containing CO and H2which is suitable for use in the synthesis of gasoline, kerosene and gas oil by, for example, the reaction system Fischer-Tropsch (FT), through the introduction of natural gas containing steam and carbon dioxide in the reformer.

In addition, since the carbon dioxide existing in the synthesis gas, is extracted to be added after preheating together with carbon dioxide, which is served separately, to natural gas containing steam, the point at the entrance of the reformer in order to be used as the source of gaseous material to the gas reformer, the amount of carbon dioxide required for the process can be reduced by carbolea, it becomes possible to suppress the carbon dioxide, which, as expected, causes global warming, when it is separated from the production installation.

Fig.4 is a block diagram illustrating the main part of the installation for synthesizing gasoline, kerosene and gas oil, which can be used in the production of synthesis gas according to the fourth embodiment. In Fig.4, the same components as in the above Fig.1, are denoted by the same numbers in order to avoid their explanations.

This installation for synthesis is characterized by the fact that the preliminary reformer 37 is located on the input side of the reformer 10. A passage for introducing the source gas 202it is reported from the upper part of the preliminary reformer 37. This preliminary reformer 37 is communicated via passage 2014with the upper part of the reaction tube 11 of the reformer 10. This passage 2014reported through the convection section 13 of the reformer 10 with the reaction tube 11. A passage for introducing carbon dioxide 204reported after passing through the convection section 13 near the radiation of the combustion chamber 12 of the reformer 10 (i.e., through the region of high temperatures inside the convection section 13) that frequent the ora intersects the passage 2014. Preferably this passage for introducing carbon dioxide 204is located so that it was reported that part of the passage 2014, which is located near the input device of the reaction tube 11.

Now the method of manufacturing a synthesis gas will be explained with reference to the above setting for the synthesis shown in Fig.4.

First of all the fuel for combustion is injected through the passage 201for the introduction of fuel radiation in the combustion chamber 12 of the reformer 10 so as to enable the fuel to burn together with the air, thus heating the inner space of the reaction tube 11 to a sufficiently high temperature (for example, up to 850-900oC). This heating of the reaction tube 11 is due to the fact that the reforming reaction in the reformer 10 is an endothermic reaction. The exhaust gas formed by combustion products containing carbon dioxide, generated in the radiation of the combustion chamber 12, provide the ability to flow through the convection section 13 in the exhaust pipe 14. When the exhaust gas formed by combustion products, passing through the convection section 13, the exhaust gas formed n the result through the passage 202for the introduction of the source gas, with natural gas containing water vapor produced in advance and passing through the passage 2014with carbon dioxide passing through the passage 204for the introduction of carbon dioxide, as well as boiling water flowing through the passage 209while cooling the flue gas formed by combustion products. The exhaust gas formed by the combustion products, chilled so, then give the opportunity to go into the atmospheric air through an exhaust pipe 14.

Natural gas containing as a main component is methane, is introduced into the passage 202for the introduction of the source gas. At this point, through the passage 203for the introduction of steam to natural gas add steam at a predetermined ratio to obtain a natural gas containing steam. By the way, regarding this pair, for example, can be used steam, which is generated during the heat exchange between the boiling water and the synthesis gas in the heat exchanger 32 (will be explained later), as well as steam, which is generated during the heat exchange between boiling water and flue gas formed by combustion products, in the convection section 13 of the reformer 10.

Natural gas containing steam, allow Postup the e can decompose hydrocarbons from C2or more high-molecular compound existing in natural gas, for example, pre-heated to 400-550o(C) when the natural gas containing steam, passes through the convection section 13 of the reformer 10, and then the natural gas containing steam, the heated, is introduced into the preliminary reformer 37. In this preliminary reformer 37 hydrocarbons from natural gas, which have two or more carbon atoms, mainly ethane, by reforming converted to methane has one carbon atom (C1), CO and H2.

Natural gas containing steam, subjected to preliminary reformer is then introduced through the passage 2014in the reaction tube 11 of the reformer 10. Carbon dioxide allow flow through the passage for the introduction of carbon dioxide 204that reported after passing through the convection section 13 near the radiation of the combustion chamber 12 with a passage 202for the introduction of the source gas. As a result, the carbon dioxide is preheated to a temperature of from 550 to 650oC, which is higher than the temperature specified above for natural gas containing steam, at a time when carbon dioxide is injected into the area of the passage 2014, which is located near the input device of the reaction tube 11 in such a way as to be mixed with the above natural gas containing steam in the reaction tube 11 may be natural gas, which is mixed with carbon dioxide and steam and is heated to a higher temperature.

The mixed gas containing natural gas, comprising as a main component is methane (CH4), steam and carbon dioxide, which is introduced into the reaction tube 11 of the reformer 10, and then is subjected to a process of steam reforming, where methane is mainly subjected to steam reforming in the presence of a catalyst inside the reaction tube 11, and the produced synthesis gas containing hydrogen, carbon monoxide and carbon dioxide at a molar ratio of H2/CO, which varies from 1 to 2.5 according to the above equations (1) and (2).

In these equations (1) and (2) for the reaction of the reformer 4 mol of hydrogen and 1 mol of carbon dioxide can be obtained by reacting 1 mole of methane and 2 moles of steam. Real reaction system, however, can be obtained a composition which is close to chemical equilibrium compositions, which can determine the population of steam and carbon dioxide to natural gas to maintain the methane content in natural gas, steam and carbon dioxide so that the molar ratio between methane (CH4) and steam (H2A) fell within: CH4:H2O=1:1.5 to 1:3; while the molar ratio between methane (CH4) and carbon dioxide (CO2) fell within: CH4:CO2=1:1-1:3.

The synthesis gas thus obtained is introduced through a passage 205in the heat exchanger 32 to thereby heat the boiling water flowing through the passage 206to generate high-pressure steam. At this time, the synthesis gas is cooled and then introduced into a device for the separation of gas and liquid 31 in which the water is separated from the synthesis gas that is allocated so the water removed from the system through the passage 207. Thus obtained synthesis gas is then transported through the passage 208in the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, a catalyst based on cobalt, with the opportunity to hydrogen and carbon monoxide contained in the synthetic gas, to interact with each other, when this happens the synthesis of gasoline, kerosene and gasoil.

In accordance with this fourth embodiment is now possible in the same way, kaeru combustion reformer, and effectively use the excess heat to the reformer for the production of synthesis gas containing CO and H2which is suitable for use in the synthesis of gasoline, kerosene and gas oil by, for example, the reaction system Fischer-Tropsch (FT), through the introduction of natural gas containing steam and carbon dioxide in the reformer.

In addition, since the preliminary reformer 37 is located before entering the reformer 10, with the possibility of pre-reforming of hydrocarbons from natural gas, which have two or more carbon atoms in methane has one carbon atom, and H2, you can reduce the heat load on the reformer 10. As a result, the amount of fuel that you must enter radiation in the combustion chamber 12 of the reformer 10 can be reduced, making possible the production of synthesis gas with the reduced amount of fuel.

Fig.5 is a block diagram illustrating the main part of the installation for synthesizing gasoline, kerosene and gas oil, which can be used in the production of synthesis gas according to the fifth embodiment. In Fig.5, the same components as in the above Fig.1, are denoted by the same numbers, C for partial oxidation in the area of the passage 205, which is located on the output side of the reformer 10 and between the lower edge of the reaction tube 11 and the heat exchanger 32. The passage 2015for introducing a gas for introduction of oxygen) communicates with the oven 38 for partial oxidation.

Now the method of manufacturing a synthesis gas will be explained with reference to the above setting for the synthesis shown in Fig.5.

First of all the fuel for combustion is injected through the passage 201for the introduction of fuel radiation in the combustion chamber 12 of the reformer 10 so as to enable the fuel to burn together with the air, thus heating the inner space of the reaction tube 11 to a sufficiently high temperature (for example, up to 850-900oC). This heating of the reaction tube 11 is due to the fact that the reforming reaction in the reformer 10 is an endothermic reaction. The exhaust gas formed by combustion products containing carbon dioxide and generated in the radiation of the combustion chamber 12, provide the ability to flow through the convection section 13 in the exhaust pipe 14. When the exhaust gas formed by combustion products, passing through the convection section 13, the exhaust gas arr is which passes through the passage 202for the introduction of the source gas, with carbon dioxide passing through the passage 204for the introduction of carbon dioxide, as well as boiling water flowing through the passage 209while cooling the flue gas formed by combustion products. The exhaust gas formed by the combustion products, chilled so, then give the opportunity to go into the atmospheric air through an exhaust pipe 14.

Natural gas containing as a main component is methane, is introduced into the passage 202for the introduction of the source gas. At this point, through the passage 203for the introduction of steam to natural gas add steam at a predetermined ratio to obtain a natural gas containing steam. By the way, regarding this pair, for example, can be used steam, which is generated during the heat exchange between the boiling water and the synthesis gas in the heat exchanger 32 (will be explained later), as well as steam, which is generated during the heat exchange between boiling water and flue gas formed by combustion products, in the convection section 13 of the reformer 10.

Natural gas containing steam, allows you to enter in the passage 202for the introduction of the source gas and pre-heated (to a temperature Pnom gas, for example, pre-heated to 400-550o(C) when the natural gas containing steam, passes through the convection section 13 of the reformer 10, and then this mixed natural gas, the heated, is introduced into the reaction tube 11 of the reformer 10. Carbon dioxide allow flow through the passage 204for the introduction of carbon dioxide, which reported after the passage area of convection section 13 near the radiation of the combustion chamber 12 with a passage 202for the introduction of the source gas. As a result, the carbon dioxide is preheated to a temperature of from 550 to 650oC, which is higher than the temperature specified above for natural gas containing steam, at a time when the carbon dioxide passes through the convection section 13 of the reformer 10. Because it is pre-heated carbon dioxide is injected into the area of the passage 204for the introduction of the source gas, which is located near the input device of the reaction tube 11, so that mixed with the above natural gas containing steam in the reaction tube 11 may be natural gas, which is mixed with carbon dioxide and steam and heated to a component methane (CH4), steam and carbon dioxide, which is introduced into the reaction tube 11 of the reformer 10, and then is subjected to a process of steam reforming, where methane is mainly subjected to steam reforming in the presence of a catalyst inside the reaction tube 11, and the produced synthesis gas containing hydrogen, carbon monoxide and carbon dioxide according to the above equations (1) and (2).

In these equations (1) and (2) for the reaction of the reformer 4 mol of hydrogen and 1 mol of carbon dioxide can be obtained by reacting 1 mole of methane and 2 moles of steam. Real reaction system, however, can be obtained a composition which is close to chemical equilibrium compositions, which can be determined by the temperature and pressure at the outlet of the reaction column.

It would be preferable in the case of adding steam and carbon dioxide to natural gas to maintain the methane content in natural gas, steam and carbon dioxide so that the molar ratio between methane (CH4) and steam (H2A) fell within: CH4:H2O=1:1.5 to 1:3; while the molar ratio between methane (CH4) and carbon dioxide (CO2) fell within: Snood 205in the furnace 38 for partial oxidation, in which the hydrogen is subjected to the reforming gas allow to burn in the oxygen introduced through the passage 2015. In this case, because subjected to the reforming gas is heated to a higher temperature, activates the generation of CO and H2O in the above reaction equation (1). Further, since the amount of hydrogen subjected to reforming gas in the furnace 38 for partial oxidation is reduced, it becomes possible to manufacture a synthesis gas having a molar ratio of N2/WITH from 1 to 2.5.

The synthesis gas obtained in the furnace 38 for partial oxidation, is inserted through the passage 205in the heat exchanger 32, in order to heat the hot water flowing through the passage 206to generate high-pressure steam. At this time, the synthesis gas is cooled and then introduced into the device 31 for separating gas and liquid. This device 31 for separating the gas and the liquid water is separated from the synthesis gas that is allocated so the water removed from the system through the passage 207. Thus obtained synthesis gas is then transported through the passage 208in the reaction system Fischer-Tropsch (FT) 33, which is filled, for example, catalysate-gas, to interact with each other, when this happens the synthesis of gasoline, kerosene and gasoil.

In accordance with this fifth embodiment of a natural gas containing steam and carbon dioxide are introduced into the reformer, and the resulting gas is subjected to reforming, is fed from the reformer into the furnace for partial oxidation, in which hydrogen contained in subjected to a reforming gas, it is possible to burn together with oxygen, separately introduced into the furnace for partial oxidation. The result is now possible to produce synthesis gas containing CO and H2which is suitable for use in the synthesis of gasoline, kerosene and gas oil by, for example, the reaction system Fischer-Tropsch (FT), and it is possible to decrease the amount of fuel that you must enter radiation in the combustion chamber of the reformer, and at the same time to effectively use the excess heat to the reformer.

By the way, the preliminary reformer, described in the above fourth embodiment, can also be used in installations for the synthesis of the above second and third embodiments.

In addition, although subjected to the reforming gas and oxygen are introduced into the furnace for partial shall be used instead. In this case, the carbon dioxide should preferably be included in the mixed gas at the ratio of 30 to 200% with respect to oxygen. When using a mixed gas containing oxygen and carbon dioxide, the interaction between hydrogen and oxygen is subjected to the reforming gas in the furnace for partial oxidation becomes slower, if there is an opportunity to minimize the possibility of an explosion.

In the present fifth embodiment is also possible to bring steam to the furnace for partial oxidation. When in the oven for partial oxidation steam is fed, it becomes possible to suppress or prevent generation of generation of free carbon, which would slow down the reaction of the FT synthesis in the oven for partial oxidation.

Bake for partial oxidation described in the fifth embodiment, can be installed in installations for the synthesis of the above second to fourth embodiments. In this case, the mixed gas containing subjected to reforming gas, oxygen and carbon dioxide, may be introduced into the furnace for partial oxidation. It is also possible in the second - fourth embodiments applying steam to the furnace for partial oxidation.

In the first to fifth waples the s to synthesize gasoline and the like. However, the synthesis gas produced in the reformer can also be used for the synthesis of methanol or dimethyl ether.

As explained above, according to the present invention is the possible introduction of natural gas containing steam and carbon dioxide and pre-heated to a high temperature in the reformer in order to reduce the consumption of fuel reformer, as well as for efficient use of the excess heat generated in the reformer. Namely, according to the present invention is possible to provide a method for production of synthesis gas, which is suitable for use in the synthesis of gasoline, kerosene and gas oil by the reaction system Fischer-Tropsch or methanol synthesis or dimethyl ether, at low cost.

Additional advantages and modifications can be easily implemented by specialists in this field. Therefore, the present invention in its broader aspects is not limited to a particular detail and presents the embodiments described above. Accordingly, various modifications may be made without deviating from the spirit or scope of the General concept of the invention, as it describes the

1. Method for the production of synthesis gas by the use of plants for the synthesis containing the reforming unit (10) having a reaction tube (11) for steam reforming, the radiation of the combustion chamber (12) formed around the reaction tube (11) for heating the reaction tube (11) by burning fuel, and a convection section (13), built with radiant combustion chamber (12), the method comprises the stage of: adding steam to natural gas to produce natural gas containing steam; passing the natural gas containing steam, through the convection section (13) reforming installation (10), thereby pre-heated natural gas containing steam; preheating the carbon dioxide by passing carbon dioxide through the convection section (13) reforming installation (10); and the introduction of the preheated natural gas containing steam and preheated carbon dioxide in the reaction tube (11), you get a synthesis gas containing hydrogen and carbon monoxide.

2. The method according to p. 1, characterized in that the carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber (12) reforming installation (10).

forming-installation (10).

4. Method for the production of synthesis gas by the use of plants for the synthesis containing the reforming unit (10) and pre-reforming-setting (37), which is provided before installation (10) during the process, the reforming unit (10) includes a reaction tube (11) for steam reforming, the radiation of the combustion chamber (12) formed around the reaction tube (11) for heating the reaction tube (11) by combustion of fuel, and a convection section (13), built with radiant combustion chamber (12), the method comprises the stages: adding steam to natural gas to produce natural gas containing steam; passing the natural gas containing steam, through the convection section (13) reforming installation (10), thereby pre-heated natural gas containing steam; introducing the pre-heated using a pre-reforming-install (37) natural gas containing steam in the reaction tube (11); pre-heating carbon dioxide by passing carbon dioxide through the convection section (13) reforming installation (10); and the introduction of carbon dioxide is preheated in the passage, which is located between the reaction tube (11) and predvaritelnogo tube you get a synthesis gas containing hydrogen and carbon monoxide.

5. The method according to p. 4, characterized in that the carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber (13) reforming installation (10).

6. The method according to p. 4, characterized in that the carbon dioxide is removed from the synthesis gas produced by the reforming-installation (10).

7. Method for the production of synthesis gas by the use of plants for the synthesis containing the reforming unit (10) and furnace (38) for partial oxidation, which provides for the reforming unit (10) during the process, the reforming unit (10) contains the reaction tube (11) for steam reforming, the radiation of the combustion chamber (12) formed around the reaction tube (11) for heating the reaction tube (11) by burning fuel, and a convection section (13), built with radiant combustion chamber (12), the method comprises the following stages: adding steam to natural gas to produce natural gas containing steam; passing the natural gas containing steam, through the convection section of the reformer installation (10), thereby preheat the natural gas containing the Oia (13) reforming installation (10); the introduction of the preheated natural gas containing steam and preheated carbon dioxide in the reaction tube (11), you get a synthesis gas containing hydrogen and carbon monoxide; introducing the synthesis gas into the furnace (38) for partial oxidation; and the introduction of a gas containing oxygen into the furnace (38) for partial oxidation, thus conducting the reaction between the synthesis gas and oxygen.

8. The method according to p. 7, characterized in that the carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber (12) reforming installation (10).

9. The method according to p. 7, characterized in that the carbon dioxide is removed from the synthesis gas produced by the reforming-installation (10).

10. The method according to p. 7, characterized in that the gas containing oxygen is the oxygen.

11. The method according to p. 7, characterized in that the gas containing oxygen, is a mixed gas containing oxygen and carbon dioxide.

12. The method according to p. 7, characterized in that the pairs are additionally injected into the furnace (38) for partial oxidation.

13. Method for the production of synthesis gas by the use of plants for the synthesis containing the reforming ustanovka, and oven (38) for partial oxidation, which provides for the installation (10) and the reforming unit (10), in the course of the process includes the reaction tube for a steam reforming unit (11), radiation of the combustion chamber (12) formed around the reaction tube (11) for heating the reaction tube (11) by burning fuel, and a convection section (13), built with radiant combustion chamber (12), the method comprises the following stages: adding steam to natural gas to produce natural gas containing steam; the passage of the natural gas containing steam, through the convection section (13) reforming installation (10) for pre-heating natural gas containing steam; introducing the pre-heated through the pre-reforming-install (37) natural gas containing steam in the reaction tube (11); pre-heating carbon dioxide by passing carbon dioxide through the convection section (13) reforming installation (10); the introduction of carbon dioxide is preheated in the passage, which is located between the reaction tube (11) and the pre-reforming unit (37)and passing the preheated natural gas containing steam in the reaction t the partial oxidation; and the introduction of a gas containing oxygen into the furnace (38) for partial oxidation, thereby making the reaction between the synthesis gas and oxygen.

14. The method according to p. 13, characterized in that the carbon dioxide is removed from flue gas formed by combustion products generated by radiation in the combustion chamber (12) reforming installation (10).

15. The method according to p. 13, characterized in that the carbon dioxide is removed from the synthesis gas produced by the reforming-installation (10).

16. The method according to p. 13, characterized in that the gas containing oxygen is the oxygen.

17. The method according to p. 13, characterized in that the gas containing oxygen, is a mixed gas containing oxygen and carbon dioxide.

18. The method according to p. 13, characterized in that the furnace (38) for partial oxidation impose additional pairs.

 

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FIELD: hydrocarbon conversion catalysts.

SUBSTANCE: catalyst for generation of synthesis gas via catalytic conversion of hydrocarbons is a complex composite composed of ceramic matrix and, dispersed throughout the matrix, coarse particles of a material and their aggregates in amounts from 0.5 to 70% by weight. Catalyst comprises system of parallel and/or crossing channels. Dispersed material is selected from rare-earth and transition metal oxides, and mixtures thereof, metals and alloys thereof, period 4 metal carbides, and mixtures thereof, which differ from the matrix in what concerns both composition and structure. Preparation procedure comprises providing homogenous mass containing caking-able ceramic matrix material and material to be dispersed, appropriately shaping the mass, and heat treatment. Material to be dispersed are powders containing metallic aluminum. Homogenous mass is used for impregnation of fibrous and/or woven materials forming on caking system of parallel and/or perpendicularly crossing channels. Before heat treatment, shaped mass is preliminarily treated under hydrothermal conditions.

EFFECT: increased resistance of catalyst to thermal impacts with sufficiently high specific surface and activity retained.

4 cl, 1 tbl, 8 ex

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