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INVENTION
Russian Federation Patent RU2270849

SYSTEM electric generating
BY GASIFICATION combustibles

Name of the inventor: Hiroyuki Fujimura (JP); ITPO Takahiro (JP); HIROSE Tetsuhisa (JP); Miyoshi Norihisa (JP); Naruse Katsutosi (JP); Hayakawa Dzuniti (JP)
The name of the patentee: Ibar CORPORATION (JP)
Address for correspondence: 129010, Moscow, ul. Boris Spassky, 25, p.3, Ltd. "Gorodissky and Partners", pat.pov. E.I.Emelyanovu
Starting date of the patent: 1999.11.05

The invention relates to electrical engineering, in particular to the technology of converting chemical energy of combustibles to electric energy with high efficiency, where combustibles are gasified to produce gas and the produced gas is used in a fuel cell to generate electrical energy. The technical result of the invention is to improve the efficiency of conversion of chemical energy into electrical combustibles. The proposed low-temperature gasification furnace for gasifying combustibles such as combustible wastes or coal is operated at a temperature of, for example, 400-1000 ° C, and the produced gas is then supplied to the fuel cell for generating electrical energy. The low-temperature gasification furnace is preferably a gasification furnace with a fluidized bed.

DESCRIPTION OF THE INVENTION

The present invention relates to a process of transformation of chemical energy of combustibles to electric energy with high efficiency, and more particularly relates to a system, electric generating system in which combustibles such as, for example, combustible wastes or coal are gasified to produce gas and the produced gas is used as a fuel gas in a fuel cell to generate electrical energy. There combustible waste includes municipal waste, fuel recovered from waste mixture solid-water, waste plastics, waste fiber-reinforced plastics (FRP), waste in the form of biomass, automobile wastes, industrial wastes such as wood wastes, low-grade coal and oily waste .

In recent years, various attempts were made to convert chemical energy of combustibles such as coal, into electrical energy. One such attempt is the system applying, generating electric energy with a combined cycle, in which combustibles are gasified under pressure for the gas, the gas obtained is used for driving the gas turbine and the heat of exhaust gas discharged from the gas turbine is utilized with using the recovery boiler to drive a steam turbine, and thus, the gas turbine and steam turbine are used in combination for power generation in combined cycle for generating electric energy with high efficiency.

However, in the above system, the electric generating, for a combined cycle gas turbine driving current must be produced gas with a high calorific value of natural gas level. That is, the existing gas turbine can not be driven with a gas having a low calorific value, obtained by gasification of combustibles having a low calorific value, such as combustible wastes such as municipal wastes. Thus, to obtain a gas with a high calorific value is necessary to take some measures, such as, for example, prevention of liquefaction of the product gas with nitrogen contained in air by using pure oxygen instead of air as a gasifying agent. As for the combustible substances with a high content of fixed carbon, such as coal, in order to fully translate into a gaseous state fixed carbon, necessary to increase the gasification temperature, as is done in OKTSG (combined gasification combined cycle).

Recently, a gas turbine has been designed for a gas with a low calorific value. However, an attempt to raise the temperature of the gas introduced to the input of the gas turbine for high efficiency requires cooling air for cooling components such as turbine blades, which are at high temperature. In the case of a gas with a low calorific value, if the relative abundance of excess air is large, then the temperature of the combustion gas decreases. Thus, the relative abundance of excess air should be limited, and therefore, the development of the gas turbine for a gas with a low calorific value provides not progress due to insufficient amount of cooling air in the given conditions.

If for gas with a high calorific value of oxygen is used, it takes energy to produce oxygen. If the temperature rises gasification reaction in order to achieve complete gasification, then additional heat corresponding to its heat content, it is necessary to thereby increase the relative oxygen content, thus resulting in a problem of reduced efficiency of the cold gas. Furthermore, because of the limitation in the gas temperature in the gas supply unit generating electrical energy, gas, which has been raised once to a high temperature, the temperature should be cooled thus disadvantageously increases the loss of heat content. For the above reason, the efficiency in terms of overall efficiency can not be increased to the extent necessary. By the expression "cold gas efficiency" as used herein refers to a value obtained by dividing the total calorific value of the gas obtained at full fuel supply heating value of the starting material.

Under these circumstances, the inventors have made the invention according to which can generate electric power with high efficiency by using combustibles having a low calorific value, as the starting material and can enrich and separate the formed carbon dioxide to suppress global warming through the optimum combination of the gas conversion technology even low calorific into electrical energy with high efficiency, sustainable technologies gas from various combustibles and removal technology components poison the fuel cell, from the product gas.

Thus, the object of the present invention to provide a system of generating electrical energy by gasification of combustibles in which combustibles such as combustible wastes or coal are gasified to produce gas and the produced gas is used in a chemical reaction to generate electricity with high efficiency .

Another object of the present invention to provide a system of generating electrical energy by gasification of combustibles in which combustibles such as wastes or coal is stably gasified in the low-temperature gasification furnace to produce gas, components poisonous fuel cell is removed from the product gas, and the purified gas is introduced into the fuel cell to generate electricity with high efficiency.

To achieve the above objects, according to one aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that combustibles are gasified to produce gas and the produced gas is then used in a chemical reaction to generate electricity.

According to another aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that combustibles are gasified to produce gas and the produced gas is then used in a fuel cell to generate electrical energy.

According to another aspect of the present invention provides a system that produces electrical energy by means of gasification of combustibles, characterized in that combustibles are gasified in a fluidized-bed furnace to produce gas and the produced gas is then used in a fuel cell to generate electrical energy.

According to another aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that combustibles are gasified to produce gas and the produced gas is reformed, and the reformed gas is then used in a fuel cell to generate electrical energy.

According to another aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that combustibles are gasified to produce gas, and the produced gas is then used in a fuel cell to generate electricity, while waste heat produced in the fuel cell It is used as a heat source for gasification.

According to another aspect of the present invention provides a system that produces electrical energy by means of gasification of combustibles, characterized in that combustibles are gasified to produce gas, and the gas obtained is used in a fuel cell to generate electricity, while exhaust gas discharged from the fuel cell, introduced into the gasification process for the exhaust gas for the gasification.

According to another aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that combustibles are gasified in a gasification combined-type fluidized bed furnace comprising a gasification chamber, the combustion chamber carbonized substances and a heat recovery chamber in one furnace to produce gas, and the produced gas is then used in a fuel cell to generate electrical energy.

According to another aspect of the present invention provides a system that produces electrical energy by gasification of combustibles, characterized in that the low-temperature gasification furnace is set for the gasification of combustibles at 400-1000 ° C, resulting in a low-temperature gasification furnace gas is fed to the unit generates an electrical energy, to generate electricity, and the exhaust gas containing a large amount of steam after the power generation is used as a gasifying agent in the low-temperature gasification furnace. According to a preferred aspect of the present invention, setting that produces electrical energy is a fuel cell.

In recent years there has been intensive development of fuel cells as a means for converting chemical energy directly into electrical energy without conversion of the thermal energy in the process. Fuel cells according to a rough classification are divided into four types, from the highest operating temperature up to the lowest operating temperature fuel cell with a solid electrolyte (SOFC) fuel cell is the molten carbonate (MCFC), a fuel cell with phosphoric acid (PAFC) and the fuel cell a polymer electrolyte (PEFC). For fuel cell and the phosphoric acid fuel cell having a polymer electrolyte requires pure hydrogen as a fuel gas. On the other hand, a fuel cell with a solid electrolyte and a fuel cell with molten carbonate have a high reaction temperature and require inexpensive metal catalyst and thus, they have the essential feature of which consists in the fact that not only the hydrogen can be used as a fuel, and carbon monoxide and which is a toxic substance for the catalyst.

Furthermore, fuel cells have the essential feature that only fuel gas components in the gas mixture can be selectively reacted. For example, even if the fuel gas such as hydrogen or carbon monoxide, is mixed with gas that is not a fuel gas such as nitrogen, carbon dioxide or water vapor, only the gas components are used as fuel in the mixed gas react with oxygen for generating electrical energy. Thus, electrical energy can be generated from a mixed gas with high efficiency without the use of any special gas separation technology.

For example, when coal or organic waste gasified with air to produce gas and the produced gas is used to drive a gas turbine to generate electricity, since the nitrogen derived from the air contained in the produced gas, an attempt to obtain a gas with a high combustion temperature requires additional heat corresponding to the sensible heat required to raise the temperature of nitrogen. Theoretically, when the calorific value of the produced gas is 3.35 MJ / m ³ (normal condition (normal temperature and pressure - NTP)) (800 kcal / Nm ^3), the combustion gas temperature is about 1500 ° C, while at calorific product gas capacity of 2.51 MJ / m ³ (normal conditions) (600 kcal / Nm ³⁾ combustion gas temperature of about 1200 ° C. However, in reality it is difficult to realize stable combustion unless the calorific value of the product gas does not exceed 4.19 MJ / m ³ (normal conditions) (1000 kcal / Nm ^3), and the high temperature combustion creates a problem of generation of thermal NOx. Thus, it is difficult to generate electricity with high efficiency by using combustion gas containing large amounts of nitrogen.

On the other hand, when a gas of the same type used for electric power generation in the fuel cell, the inclusion of nitrogen in the product gas, i.e. fuel gas, has some negative effects, such as reducing the frequency of interaction with components of the fuel gas electrode, but this adverse effect is significantly weaker than the negative effect in the case of power generation by a gas turbine.

When combustibles with low calorific value, such as municipal wastes having a calorific value of about 8.37 to 12.56 MJ / kg (2,000-3,000 kcal / kg) are gasified to generate electricity, it is important to improve the efficiency as much as possible cold gas. In the developed gasification and slagging combustion technology for waste treatment in some cases, a method of indirect heating, such as, for example, for the external heating in the pyrolysis furnace. This is precisely "in order to avoid partial combustion and improve the cold gas efficiency with limited relative abundance of oxygen." The most effective way to improve the efficiency of the cold gas is useless in preventing generation of heat. Specifically, it is effective as high as possible lowering of the gasification temperature. When the gasification temperature can be lowered, it may be reduced and the amount of fuel consumed material to generate heat to raise the temperature, and oxygen consumption. This can improve the efficiency of the cold gas, and even when an oxidizing agent is pure oxygen is used, the energy involved in the production of oxygen can be reduced, and hence, increases the efficiency of the "end of transmission".

The use of low-temperature gasification furnace and is favorable for the material. The process to complete gasification of coal (OKTSG), which is currently being developed, the maximum temperature gasification furnace is about 1500 ° C or higher. Therefore it is very difficult to select a refractory material which can withstand such high temperature. Currently there is no refractory material that can withstand such operating conditions and the temperature and thus to extend the service life of the refractory material is cooled from the outside. For this reason, even when the size of the furnace is reduced by applying a high pressure system, the radiation loss from the surface of the furnace wall reach several% of the total heat input, thereby causing an increase in "overhead" in the general efficiency.

When the gasification temperature is decreased, then there is no complete decomposition of the combustible component, it causes that hydrocarbons whose molecular weight is relatively large, and high molecular weight hydrocarbons such as tar out instead of hydrogen and carbon monoxide as a component of the fuel gas to the fuel cell. When these high molecular weight hydrocarbons are fed to the fuel cell, without removal from, they are used as fuel, which results in not only a decrease in the efficiency, but also causes the condensation polymerization reaction of carbon deposition within the cell. Thus, higher hydrocarbons are the source of various problems.

However, in recent years we studied various catalysts for accelerating the complete gasification at a relatively low temperature of 700 to 800 ° C. The result found that are effective not only nickel, but also sodium, potassium, calcium, FeO and other catalysts. In addition, fuel elements having a high operating temperature, such as a fuel cell with a solid electrolyte (SOFC) fuel cell and a molten carbonate (MCFC), characterized in that they occur in the "samoteplovoy" reformer fuel gas, i.e. an internal reforming fuel gas can be accomplished by the use of their high operating temperature and heat of combustion of the residual fuel gas, which goes inside without using a fuel cell. When the function of the internal reforming can be effectively used, whereas gas produced by gasification at a relatively low temperature, can be used as fuel gas in the fuel cell.

The catalysts described above are intended to decomposition of the resin and hydrocarbons contained in the gas obtained in the gasification process, into hydrogen and carbon monoxide, that is, they perform a so-called "reformed function". In this case, the reformer can be achieved by maintaining the catalyst bed at a predetermined temperature and by introducing the obtained gas containing a hydrocarbon resin and, together with the reformed gas such as carbon dioxide or water vapor in the layer. Temperature layer containing a catalyst, usually in the range of 700 to 800 ° C. Although the catalysts described above have catalytic activity, the same as a simple metal, many of them, even when they are moving to the oxides (e.g., CaO in the case of calcium), have the same function. These catalysts may be used as a gasification furnace of the fluidized medium of the fluidized bed.

In this connection it should be noted that if the gas obtained from various combustible substances, is used as fuel gas in the fuel cell, sufficient attention should be paid to the corrosive gases contained in the produced gas, such as hydrogen chloride or hydrogen sulfide. Specifically, the fuel cell with a solid electrolyte (SOFC) and a fuel cell with the molten carbonate (MCFC) having a high operating temperature, exposed to certain corrosive conditions, and thus, before the gas obtained is fed to the fuel cell, the above-mentioned corrosive gases should be removed.

When the obtained gas containing hydrogen chloride or hydrogen sulfide, the process for the removal of corrosive gases can be used effectively "packed" layer "fast" lime (CaO). Hydrogen chloride reacts with the "fast" lime to produce calcium chloride (CaCl _2), and the hydrogen sulfide is reacted with a "fast" lime to produce calcium sulfide (CaS). Thus, if there is a "stuffed" layer "fast" lime downstream of the gasification process in which the obtained hydrogen sulfide or hydrogen chloride, then the aggressive components can be removed without significantly reducing the gas temperature.

Further attention should be paid to the alkali metal salts such as sodium chloride (NaCl) and potassium chloride (KCl), as the aggressive components which create corrosion problems in the gasification of municipal waste or other similar materials. These alkali metal salts are in the form of mist in the molten state in a temperature range of 650 ° C or higher, and they have a tendency to adhere to parts having a temperature lower than their melting temperature, thus leading to severe corrosion. Thus, it is important to protect the metal structural elements of the fuel cell from corrosion of these molten salts. Molten alkali metal salts can be effectively removed from the product gas by a single cooling of the product gas to a temperature below the melting salts, salts to harden, and they are derived by a filter or other similar means.

Since the melting temperature of the alkali metal salts of 650 ° C or above, cooling the gas to a temperature below 650 ° C, followed by a thin abatement, such as dust removal through a ceramic filter, can greatly reduce the risk of corrosion by molten salts. The temperature of 650 ° C and is very advantageous in the processing of the produced gas containing tar or other similar substances. This is because the resin is in the gaseous state at a temperature of 400 ° C or higher, and such a problem as the resin filter blockage occurs.

According to a preferred aspect of the present invention, combustibles are gasified in the low-temperature gasification furnace at a temperature of from 400 to 1000 ° C to produce gas and the produced gas is cooled to 650 ° C or below, and then passed through a gas cleaning apparatus for removal of toxic components and further purified product gas is supplied to the fuel cell for generating electrical energy. In this case, the solid components such as ash, carbonized, contained in the gas and salts, which is output from the low-temperature gasification furnace and cooled to 650 ° C or lower are captured using the dust collector located at an average temperature, to prevent ingress of solids in gas treatment apparatus installed in a subsequent process step. Prior to purification of the product gas with a gas purification apparatus, the produced gas may be heated to a high temperature of 1000-1500 ° C to decompose the resin and the hydrocarbon contained in the produced gas, to low-molecular material and then the produced gas can be supplied to the fuel cell.

gas purifying apparatuses can be classified into two types: dry type and wet type. In the case where the fuel cell is a fuel cell with a solid electrolyte or fuel cell with molten carbonate, using gas purification apparatuses dry type, after cooling the product gas to 650 ° C or lower is effective for preventing the loss of heat content as the operating temperature of the fuel cell with a solid the electrolyte is in the range from 900 to 1000 ° C, and the temperature of the fuel cell with molten carbonate about 700 ° C. On the other hand, if the fuel cell is a fuel cell with phosphoric acid or a fuel cell polymer electrolyte fuel gas temperature is supplied to the fuel cell must be reduced to 200 ° C or below, since the operating temperature of the fuel cell with phosphoric acid, 200 ° C, and the temperature of the fuel cell polymer electrolyte, about 80 ° C. For this reason, gas cleaning at a high temperature is not required and can be applied wet gas cleaning apparatus type. Therefore, as a means for removing alkali metal or the resin components in order to perform water washing gas, a scrubber can be used.

The basic structure of the system generating electrical energy by gasification of combustibles according to the present invention will be described with reference to fig.23-25. On fig.23-25 ​​similar or corresponding elements are designated by the same reference numerals to avoid repetition of explanation.

23 is a diagram showing the basic structure of the present invention. Combustible materials are supplied to carry out the process A and gasified in the gasification process A gasification. The gas produced in the gasification process A is cooled to 650 ° C or lower when the process in the heat recovery. If necessary, it may be provided dedusting process 3 above and / or downstream of the heat recovery process. The gas cooled in the heat recovery process B is supplied to the process C cleaning gas, where the gas is cleaned, becoming a fuel gas for a fuel cell. Then, fuel gas is supplied to perform process 6 via the power generation of the fuel cell.

24 is a diagram illustrating the structure of the first process gas purification C. When introducing the product gas for performing gas purification process C corrosive gases such as hydrogen chloride and hydrogen sulfide are removed from it when the process 4 removing corrosive gases. The treated gas is then introduced to carry out the fuel reforming process 5 to effect decomposition of hydrocarbons into hydrogen and carbon monoxide, and supplied to the execution process 6 by using the power generation of the fuel cell. It should be noted that in the gasification process, when the high-temperature gasification furnace operated at a temperature of 1000-1500 ° C, is set apart from the low-temperature gasification furnace, and it may be a complete decomposition of hydrocarbons, while the fuel reforming process 5 may be omitted. The fuel reforming process may be used a fixed bed reactor, "stuffed" reformed catalyst described above, or a moving bed, or a reformer with a low-temperature plasma, which can selectively degrade hydrocarbons without substantially increasing the gas temperature. A reformer, which uses low-temperature plasma has an advantage that there are no significant limitations on the operating temperature and operating pressure. This first structure for gas purification process is suitable in the case where a fuel cell having a relatively high operating temperature, i.e. a fuel cell having a solid electrolyte fuel cell or a molten carbonate. Selection dry type process using iron oxide or zinc oxide as an absorbent in the removal of corrosive gases, produces a purified gas feed 6 for its power generation process using the fuel cell without any loss of heat content of the produced gas.

25 is a diagram illustrating the structure of the second process gas purification C. This structure of the second process gas purification C is suitable in the case where the fuel cell is a fuel cell or a polymer electrolyte fuel cell with phosphoric acid. With the structure shown in Figure 25, by introducing the gas obtained in the gas purifying process C, corrosive gases such as hydrogen chloride and hydrogen sulfide, are removed in the implementation process 4 removing corrosive gases, and the resulting gas is then introduced to the process of fuel reforming process 5, where hydrocarbons are decomposed into hydrogen and carbon monoxide. The treated gas is introduced into the process 17 for conversion where carbon monoxide is converted into hydrogen using a CO shift reaction. The gas is then introduced to carry out process 18 removing CO to remove residual carbon monoxide, and then the gas passes through process 19, the purification of hydrogen using a hydrogen absorbing alloy, to produce pure hydrogen or gas highly hydrogen, which is then fed to the implementation process 6 power generation using the fuel cell. If the fuel element can be coated with a gas, depleted in hydrogen, while the hydrogen treatment process may be omitted. The particular structure of process removing corrosive gases 4 such that the hydrogen chloride is removed in the gas purification process wet type scrubber or employing other similar means, the desulfurization process using a hydro desulfurization is performed downstream of the wet gas purification process type. To perform the process of removing corrosive gases and a combination of other methods may be used. In some cases, effective to provide a pretreatment process upstream of the process 17 and process 18, conversion of CO removal. The technological process for reducing the carbon dioxide partial pressure in a gas or increasing the partial pressure of water vapor in the gas to accelerate the conversion reaction is effective as a pretreatment for the conversion process. Specific examples of pretreatment methods used herein include amine absorption method, in which carbon dioxide is absorbed to reduce the partial pressure of carbon dioxide, and a method in which steam is injected into the product gas to increase the partial pressure of water vapor. Methods that are used as pre-treatment process for removing CO process 18 are different depending on the method for removing CO. Specifically, when as a method for removing CO is used methane formation process using methane producing reaction, then, while minimizing the content of carbon dioxide for effective absorption of carbon dioxide is method amines. On the other hand, when a method is used for removing CO selective oxidation process utilizing a selective oxidation must then injected oxygen-containing gas as the oxidizing agent. While the CO and can be removed by low temperature plasma, in this case blown steam.

- DRAWINGS illustrate the invention -

Embodiments system generating electrical energy by gasification of combustibles according to the present invention will be described with reference to fig.1-22. Fig.1-22 on similar or corresponding elements are designated by the same reference numerals to avoid repetition of explanation.

1 - schematic diagram illustrating a basic structure of the system, generating electricity, a fuel cell combined-cycle according to the first embodiment of the present invention. Starting material 21 is fed through the apparatus 1 for feeding the starting material in a low-temperature gasification furnace 2, the gasification furnace which is a fluidized bed. In the furnace, pyrolysis of the starting material 21 at a temperature ranging from 400 to 1000 ° C to obtain a gas containing hydrogen and carbon monoxide as a gas component, which is useful for power generation by a fuel cell and gas contains a "trace" amount of hydrocarbons . In this case, the temperature rise of the temperature, which was entered during the starting material to a temperature in the range of 400-1000 ° C is carried out by partial combustion of the starting material 22, 21. Non-combustible substances contained in the raw material 21 discharged from the low-temperature gasification furnace 2. gasification furnace can be a fluidized bed furnace, or alternatively may be a rotary kiln, furnace, or similar drive oven. When used as a starting material combustible materials such as municipal wastes that are irregularly shaped and contain combustible material, while it is desirable to use a fluidized bed furnace. This is because in the fluidized bed furnace are not burnt material does not adhere to the non-combustible substances, which are discharged from the kiln, hence, with less likely to cause problems associated with handling and disposal of non-combustible materials. Furthermore, when used with a fluidized bed furnace, the temperature of the layer is preferably low to such an extent that it does not interfere with the pyrolysis. Specifically, the furnace is preferably operated at a temperature of 400 to 600 ° C, since the incombustible material is not oxidized and therefore, they can be easily reused.

When used as a starting material combustible materials such as municipal wastes, having irregular shapes, the raw material supply device as shown in Figure 16, it is preferably configured to prevent air leak through the apparatus for supplying starting material. The apparatus for supplying starting material shown in Figure 16, will be described in more detail. External device 1 casing for supplying the starting material contains bunker section 401 for the source material, the housing 402 which has a tapered shape so that its diameter gradually decreases toward the front end, a tapered perforated casing 403 having a plurality of holes 430 and located downstream of the conical casing 402 and the front cover 404, including the release screw 450. The housing 410 is provided, the diameter of which gradually decreases toward the front end so that it matches the cone-shaped casing. Combustible matter 21 serves as the starting material in the bunker section 401 for starting material and transferred to a front end of the screw by the rotation of the screw 410. At the same time, combustible materials are compressed due to the conical configuration of the screw 410 and the housing 402. The water contained in the compressed combustible squeezed substances and discharged to the outside of the device for feeding raw material through multiple openings 430 formed in the housing 403. the size of the openings is small enough to eliminate combustibles output through these holes, and the maximum hole diameter of about 10 mm. Combustibles having a decreased water content as a result of compression are supplied through the outlet 450 in the low-temperature gasification furnace 2.

In the apparatus 1 for starting material supply combustibles are compressed in housings 401, 402 and 403 to thereby increase the internal pressure of the apparatus 1 for feeding a raw material and, therefore, air or other such components do not come from the outside into the device 1 . Furthermore, the crimp reduces the water content in the combustible materials and therefore reduces heat loss in the low-temperature gasification furnace, resulting "latent" evaporation heat. The relative content of oxygen is lowered because of reduced heat losses, which increases the efficiency of the cold gas. Compressed combustibles have a relatively uniform density, which may reduce small fluctuations in the amount of feed material. Thus, the device 1 for supplying the starting material shown in Figure 16 is very suitable for use in the present invention as an apparatus for supplying starting material.

The simplest method of processing the squeeze of raw materials derived material in compression with a device for supplying raw material, is that the squeeze of raw materials is fed into the heat recovery process B (see. Figure 23), where the squeeze of raw material is mixed with the resultant high temperature gas going to evaporation and decomposition. However, if the squeeze starting material can not be fed into the process in the recovery of heat from the thermal balance or for other reasons, then squeeze the starting material may be fed into the process to perform the drying process by drying treatment. In a preferred method of drying treatment by a dryer is used with indirect heating. The heat generated in the fuel cell 6, is the most suitable source of heat for drying from the viewpoint of efficient use of heat. In the case where the heat transfer surface must be large due to the low temperature level (100 ° C or below) of the exhaust gas as a fuel cell polymer electrolyte, it may then be used heat retracted from the product gas in the process in the heat recovery. When the amount of heat is insufficient, an auxiliary fuel is added. The remaining solid component after drying may be mixed with the raw material for processing. Steam generated during a drying of the squeeze of raw materials, has an unpleasant odor and therefore is preferably supplied to the process in the heat recovery, where the steam is mixed with the high temperature product gas, to a decomposition occurred. Thus, if, after evaporation and drying the resulting squeeze of raw materials out of the system with the product gas in the process of heat recovery process applied only formed vapor then assumed that advantageously carried out blowing of the squeeze of raw materials directly into the heat recovery process, because the magnitude of reduction of the gas temperature is so low that in the process of heat recovery can be increased by the amount of generated steam. Specifically, in the case where a gasification process using the high-temperature gasification furnace operated at a temperature of 1000-1500 ° C, and the process of heat recovery process is carried out downstream of the high-temperature gasification furnace, such a system is advantageous. This is because the temperature of the produced gas introduced into the heat recovery process technology, high, approximately 1300 ° C, heat transfer in the heat recovery process is carried out by radiation heat transfer and thus while maintaining a high gas temperature is obtained a greater degree of increase in the amount of recovered heat.

The resulting gas, solid components such as ash derived from the low-temperature gasification furnace 2 are fed to the dust separator 3. At this time, the dust collector inlet temperature is maintained at 400-650 ° C. The part located downstream in the low-temperature gasification furnace 2, i.e. in the "freeboard" portion, the gas temperature lower than the temperature in the fluidized bed due to the fact that the endothermic pyrolysis reaction occurs. Therefore, even if the temperature of the fluidized bed 950 ° C, there is a possibility that the "topside" portion of the gas temperature is lower than 650 ° C. When the gas temperature is high, the radiation boiler may be provided. On the other hand, when the gas temperature is 400 ° C or lower, to raise the gas temperature in the "freeboard" part can be supplied, air or oxygen, thereby avoiding problems with tar. The cyclone dust collector can be used as a. However, it is desirable that the filtering system has been implemented, which has a high dust collecting efficiency. In the temperature range from 400 to 650 ° C can be used as a high-temperature dust collector baghouse. Alternatively, there may be used a ceramic filter or the like, which are being developed extensively.

The resulting gas, from which solid components such as ash and alkali metal salts 23 are removed in the dust separator 3, 4 is fed into the machine remove corrosive gases where corrosive gases such as hydrogen chloride and hydrogen sulfide are removed from the product gas. As an apparatus for the removal of corrosive gases is effective to the above layer containing the "fast" lime. For example it may be used with moving-bed dust collector which uses a "fast" lime or similar substance, as shown in Figure 11. This system has a dust collector function and the function of removing corrosive gases and therefore, it can simplify the equipment as a whole. The medium for the formation of a moving bed dust collector comprises a moving bed dolomite, in addition to the "fast" lime. To remove sulfur components is performed a process in which all sulfur components are converted in the presence of a catalyst based on Ni-Mo in the hydrogen sulfide and hydrogen sulfate obtained is reacted with zinc oxide (ZnO) to obtain zinc sulfide (ZnS), which is then output.

Next, a dust collector moving bed shown in Figure 11. The dust collector 150 comprises a moving bed enclosure 151, within which is contained a filter 152. The filter 152 has a layer 153 packed with particles of CaO and CaO particles circulate between the filter 152 and the regenerator 154 for external circulation path 155. The product gas discharged from the dust collector 3 (see FIG. 1) enters the dust collector 150 through an inlet 151a in the housing 151 and flows into the filter 152. The filter 152 of hydrogen sulfide (H ₂ S) and hydrogen chloride (HCl), contained in the product gas are removed due to their interaction with CaO, and the resulting purified gas is withdrawn through the outlet 151. the housing 151b chemical reaction formula in this case is as follows:

H ₂ S + SaO-> CaS + H ₂ O

2HCl + SaO-> CaCl ₂ + H ₂ O

CaO remaining unreacted, and the products of chemical reaction (CaS and CaCl ₂₎ are supplied to the regenerator 154 where CaS removed and CaCl ₂ and CaO only returned to the filter 152 by circulating path 155. Through the circulation path 155 is updated CaO amount that has been consumed in the reaction with hydrogen sulfide and hydrogen chloride.

The apparatus 4 for removing aggressive gases containing dust collector 150, a moving bed, or other similar means, the produced gas from which the removed corrosive gases, is fed into the unit 5 to the fuel reforming wherein hydrocarbons contained in the produced gas are decomposed into hydrogen and carbon monoxide. To accelerate the decomposition requires a high temperature, and hydrogen and carbon monoxide contained in the gas extracted from the anode (negative electrode) in the fuel element, effectively used as a heat source to provide heat. Therefore, if necessary, oxygen (O ₂₎ 31 is supplied to the device 5 to the fuel reformer, tail gas to burn.

12 is a schematic cross sectional view showing a detailed structure of a device 5 for fuel reforming. Apparatus for fuel reformer 5 comprises a body 190 and reaction tube 191 mounted within the housing 190 and packed with a catalyst based on Ni-Mo or Co-Mo-based acceleration to reduce the molecular weight hydrocarbons. The resulting gas and if necessary hydrogen to the steam reformer and as a source of oxygen fed to the reaction tube 191. The fuel gas contained in the exhaust gas extracted from the anode, and oxygen is fed again fed into the combustion chamber 192 for burning the fuel gas. The reaction tube 191 is heated to about 800 ° C due to the heat obtained by the combustion reaction, thereby completely carried decomposition of hydrocarbons contained in the produced gas, hydrogen and carbon monoxide.

The resulting gas, which consists mainly of hydrogen and carbon monoxide obtained by gasification in the gasification furnace 2, a fuel gas composed of hydrogen and carbon monoxide produced by the decomposition of high-molecular hydrocarbons in the apparatus 5 for fuel reforming, steam and carbon dioxide is fed by a negative electrode in the fuel cell 6 with the molten carbonate (MCFC) for generating electrical energy. At this time, the air or oxygen 32 serves as a source of oxygen from the positive electrode in the fuel cell 6. Normally, since the conversion ratio of the fuel gas in the fuel cell is not 100% when the exhaust gas discharged from the negative electrode side of the fuel cell 6 contains a small amount of unreacted fuel gas (composed of hydrogen and carbon monoxide) in addition to steam and carbon dioxide as the main components, and the exhaust gas is used as heat source for reforming fuel gas.

The temperature of the exhaust gas discharged from the negative electrode side of the fuel element is substantially equal to the operating temperature of the fuel cell. Therefore, this heat content can be reused as a heat source for gasification, to thereby reduce the amount consumed in the partial combustion of combustibles. Advantageously, the gasification efficiency can be increased and, moreover, due to the high content of steam in the exhaust gas gasification reaction rate can be increased by the conversion effect of the steam. The exhaust gas discharged from the negative electrode side of the fuel cell 6 contains a small amount of unreacted fuel gas (composed of hydrogen and carbon monoxide) in addition to water vapor and carbon dioxide as the main component. According to the present embodiment, the high-temperature blower 9 is used to reuse an exhaust gas having a temperature of 600 to 700 ° C, discharged from the negative electrode side of the fuel cell. This gas is used as a gasifying agent and a fluidizing gas for the low-temperature gasification furnace 2. When the heat content itself recycle gas sufficient to maintain the temperature of the layer of low-temperature gasification furnace 2, then, if necessary, the low-temperature gaeifikatsionnuyu furnace 2 can be supplied to the oxygen (O ₂₎ 31. in this case, considering the supply of oxygen, oxygen is mixed in the circulating gas will facilitate combustion of the remaining combustible gas, hence the temperature will rise. Therefore, the oxygen and recycle gas are preferably fed each independently to the low-temperature gasification furnace 2. Furthermore, the supply of oxygen having the purity of 100%, is dangerous because of its extremely high activity, and therefore, it is desirable that oxygen is supplied, which is thinned with water steam, carbon dioxide, or something similar.

In the fuel cell, molten carbonate (MCFC), as necessary to supply the carbon dioxide in the positive electrode, a part of the exhaust gas discharged from the negative electrode side is supplied to the gas the gas combustion chamber 7 for complete combustion of combustible substances and a part of the gas obtained by combustion gas is cooled in the cooler 8 to remove water therefrom (H ₂ O) 36, thereby producing carbon dioxide (CO ₂₎ 35 having a high degree of purity. The required amount of carbon dioxide 35 is supplied through the plenum 12 to the positive electrode of the fuel cell 6, and the remaining portion of the carbon dioxide 35 is expelled from the system. Deduced carbon dioxide having a high purity can be used as chemical reagents for other applications. The carbon dioxide may alternatively be "linked" to prevent the release of carbon dioxide, thus taking measures to prevent global warming. The remaining gas after complete combustion discharged from the combustion gas chamber 7 together with the exhaust gas discharged from the positive electrode of the fuel cell is supplied to the waste heat boiler 10 where heat is recovered and utilized as a heat source for the steam cycle. The exhaust gas from the recovery boiler 10 is expelled out of the system through the plenum 11. The heat produced in the gas combustion chamber 7, and can be effectively used as a heat source for the reforming of fuel.

2 is a diagram illustrating the structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to a second embodiment of the present invention. The electric power generation system of a fuel cell combined-cycle corresponding to the embodiment shown in Figure 2, the device 5 for reforming fuel, the fuel cell 6 and the gas combustor 7 combined to simplify setup and to increase efficiency. Such association allows for efficient use of fuel reforming heat produced in the fuel cell 6 and 7 of the combustion gas chamber, and thus, it is effective to increase the overall efficiency. The rest of the structure of the embodiment shown in Figure 2, is the same as in the embodiment shown in Figure 1.

When combustibles having a low calorific value, such as municipal wastes are gasified by means of the process, shown in Figure 2, the calorific value of the product gas is low, 1,88-2,10 MJ / m ³ (normal conditions) (450 500 kcal / Nm ³⁾ on the basis of wet gas and about 2.72 MJ / m ³ (normal conditions) (650 kcal / Nm ³⁾ on the basis of dry gas. The resultant gas contains about 13% hydrogen by volume and about 3% by volume of carbon monoxide as an effective gas component and the remaining component consists of water vapor and carbon dioxide. Using gas having the above chemical composition, energy generation in the fuel cell produces a problem in that because of the low content of the effective gas efficiency of interaction effective gas with the electrode is so low that the effective use of the fuel gas within the fuel cell decreases and the performance element can not be sufficiently used, which results in reduced output settings. In this case, an increase in pressure in the system is effective in solving this problem. Namely, the pressure increase can increase the effective partial pressure of gas, to increase the effectiveness of the electrode an effective interaction with the molecules of gas and thus increase the efficiency of the fuel gas ratio.

Furthermore, increasing the fuel gas component partial pressure may result in not only an increased coefficient of efficiency of the fuel gas, but also to improve the efficiency of power generation by the fuel cell itself. Furthermore, increased pressure can reduce the amount of fuel gas, thus contributing to the implementation of the "compact" process for gas purification.

a method in which gasification furnace per se is operated under pressure, and a method in which the gasification is carried out at atmospheric pressure and then the resulting compressed gas: The following methods as a method of increasing the fuel gas pressure supplied to the fuel cell addresses. In the first method we have a difficulty with the starting material feed system under elevated pressure, and is particularly difficult to load into a pressurized section of combustibles having irregular shapes, such as domestic waste. On the other hand, in the latter method to reduce compression energy of the gas must be cooled before the compression and hence loss occurs unfavorable enthalpy increase by an amount corresponding to the degree of temperature reduction. In the case where a fuel cell is used as a fuel cell polymer electrolyte (PEFC) or a fuel cell with phosphoric acid (PAFC), in any case, the feed gas temperature should be lowered. Where applicable the fuel cell with the molten carbonate (MCFC) or a fuel cell with a solid electrolyte (SOFC), despite the fact that it can be fed a high-temperature gas, this gas is once must be cooled to compress, thus resulting in energy loss .

Therefore, when the fuel cell is used as MCFC or SOFC, preferably, the gasification furnace itself is operated at elevated pressure. On the other hand, when the PEFC and PAFC is used, taking into account the above drawback most suitable gas compression method can be selected and adapted to each specific system. Although it is theoretically desirable that the fuel gas pressure supplied to the fuel cell was higher, from the viewpoint of practical use and construction of a fuel cell which is resistant to the elevated pressure, the fuel gas pressure supplied to the fuel cell is in the range of 0.2 to 1.0 MPa, preferably from 0.4 to 0.8 MPa, and more preferably from 0.5 to 0.6 MPa. In this case, the working pressure in the gasification process to be 5-50 kPa higher than the normal pressure applied to the fuel cell. When the fuel gas pressure is increased by a compressor to supply the fuel gas to the fuel cell, the gasification process can be performed at any pressure. However, given the starting material supply to the gasification furnace is desirable that gazifiktsionnaya furnace was operated at a pressure lower than the atmospheric pressure of 0.2-1.0 kPa.

3 is a diagram illustrating the structure of the system, generating electricity, a fuel cell combined-cycle plant according to a third embodiment of the present invention. The third embodiment, shown in Figure 3 - is a variant in which the fuel gas is pressurized. In the present embodiment, the fuel cell 6, the device 5 for fuel reforming, gas combustion chamber 7, a gas cooler 8, the apparatus 4 for removing corrosive gases, dust collector 3, and the low-temperature gasification furnace 2 are at high pressure conditions in the reservoir 13 pressurized. In this case the source material to be supplied from the system under atmospheric pressure, a system under high pressure, and therefore, the preferred starting material in feeding the low-temperature gasification furnace 2 through a loading device with a funnel-gate or other similar device. Combustibles having irregular shapes, such as municipal wastes, are likely to cause problems when loading through funnel part loading device. For this reason, this system is suitable for use of combustibles having a nature such that they are easily processed. For example, RDF, obtained by removal of non-combustible materials from urban waste, and molding and drying and combustibles remaining in the solid fuel, and tire crumbs are suitable fuel for this system.

When the power generation in the fuel cell is carried out at elevated pressure, as in the present embodiment, when the fuel cell of the molten carbonate (MCFC) displayed a high pressure gas having a temperature of about 700 ° C. Therefore, the exhaust gas discharged from the fuel cell 6 can be introduced into the gas turbine (gas expander) 14 to receive the energy via a gas turbine 14. The exhaust gas discharged from the gas turbine 14 is supplied to the HRSG 10, where heat recovery is carried out heat, and the resulting steam enters the steam turbine for power generation. Thus, a three-stage combined-cycle power generation can be realized by using the fuel cell 6, the gas turbine 14 and steam turbine (not shown). 3, only one high-pressure vessel 13 is provided throughout the system. Alternatively, multiple high pressure reservoirs may be provided as devices placed inside the high pressure tanks, respectively. The rest of the structure of the embodiment shown in Figure 3, is the same as in the embodiment shown in Figure 2.

Another system can be used to combustibles having a high calorific value, such as waste plastic. In recent years, due to the limitation of seats dumping and other such places is increasing demand to ensure that the re-use of slag resulting from the slagging furnace waste incineration. Combustible materials of high calorific value, such as plastic waste, have a sufficiently high calorific value to perform slagging contained ash or to increase the temperature of the product gas to reduce the molecular weight of the produced gas, and thus it can be used in various technological processes .

4 is a diagram illustrating the structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to a fourth embodiment of the present invention. The fourth embodiment shown in Figure 4 - a variant, wherein the power output of a fuel cell in a combined cycle is carried out using as starting material combustibles having a high calorific value, such as waste plastic. Starting material 21 is pyrolyzed and gasified at a temperature of 400-1000 ° C in a low-temperature gasification furnace 2 to produce gas and the produced gas is supplied into the high temperature gasification furnace 15. In the high-temperature gasification furnace 15 further gasified product gas at a temperature of 1000-1500 ° C lowering the molecular weight of the produced gas. The high-temperature gasification furnace 15 is maintained at the melting temperature of the ash contained in the produced gas, or at a higher temperature. Thus, 80-90% ash contained in the produced gas is converted into slag, and the slag is discharged as molten slag 26 outside of the system. Uglevodrody and organic substances contained in the produced gas are completely decomposed in the high-temperature gasification furnace into hydrogen, carbon monoxide, water vapor and carbon dioxide. The gas produced in the high-temperature gasification furnace 15 is then cooled to 650 ° C or below in a waste heat boiler, which is a radiation boiler 16, to solidify molten alkali metal salts. Alkali metal salts 24 after the solidification are collected by the dust collector 3. On the other hand, steam 36 produced in the recovery boiler is supplied to a steam turbine to generate power.

The low-temperature gasification furnace is operated in a temperature range of 400 to 1000 ° C, preferably 450-800 ° C, and more preferably from 500 to 600 ° C. The high-temperature gasification furnace is operated in a temperature range from 1000 to 1500 ° C, preferably from 1000 to 1400 ° C, and more preferably from 1100 to 1350 ° C.

The produced gas after the complete decomposition of the organic material and removing the solid material fed into the unit 4 removing corrosive gases, in which corrosive gas is removed. The resulting gas, after removal of corrosive gas used in the fuel cell 6 to generate electricity. In this process the high temperature gasification furnace 15 has two functions for fuel reforming and ash slagging. Such a process has the great advantage, since the ash can be converted into a slag, and then withdrawn separately from the alkali metal salts and metals having a low melting point, thus contributing to reducing the problems associated with the removal of ash. Moreover, the fuel reformer may be expelled directly to the fuel cell. However, this process has drawbacks in that the produced gas which has been once heated to 1000 ° C or higher should be cooled to a temperature of 650 ° C, which is lower than the solidification point of molten salts of alkali metals. Since the high temperature product gas still contains a large amount of corrosive components, despite high-temperature sensible heat, heat must be recovered from the formation of low-temperature steam. This adversely reduces the efficiency in proportion to the degree of temperature reduction.

However, in recent years, the technology of high enthalpy recovery of 700 ° C or higher from the high-temperature gas, using a gas such as air as a medium for heat recovery. Oxygen, water vapor or the like is used as a gasifying agent to the low-temperature gasification furnace is used as a heating medium, and after heating to 700 ° C or higher, the heating medium is supplied to the gasification furnace for efficient use of high heat content.

Part of the exhaust gas discharged from the negative electrode side of the fuel cell 6 is fed to the low-temperature gasification furnace 2 through a high-temperature blower 9 re-use of the exhaust gas as a gasifying agent and a fluidizing gas. The exhaust gas discharged from the negative electrode side of the fuel cell 6, and is supplied to the gas combustor 7 and the high-temperature gasification furnace 15.

At this time, it is advisable that instead of the radiation boiler 16 downstream of the high-temperature gasification furnace 15 has been installed apparatus for the recovery of high-temperature sensible heat and indirect heat exchange is performed between high-temperature gas and a part of exhaust gas discharged from the negative electrode side of the fuel cell 6 to high-temperature sensible heat recover high-temperature gas, which is then returned to the low-temperature gasification furnace 2. When a part of the exhaust gas discharged from the negative electrode in high-temperature gasification furnace is important that the exhaust gas is mixed with oxygen containing gas, while the exhaust gas flows into the high-temperature gasification furnace . Nozzle for supplying exhaust gas discharged from the negative electrode, and a nozzle for supplying an oxidizing agent at high temperature established gazitsikatsionnoy furnace must be installed separately. When the exhaust gas and oxidizing agent should be fed inevitably through one nozzle, the nozzle is then used for two fluids having a structure with two tubes, so that the exhaust gas discharged from the negative electrode side and the oxidizing agent are mixed with each other within the furnace.

On the other hand, exhaust gas discharged from the positive electrode side of the fuel cell 6 is supplied into the gas combustor 7 and the waste heat boiler 10. After the combustible substances contained in the exhaust gas are burned in the gas combustion chamber 7, part of the exhaust gas, derived from combustion of the gas chamber 7 is connected with the exhaust gas from the recovery boiler 10 and the combined exhaust gas is discharged outside the system through the plenum 11. Another part of the exhaust gas discharged from the gas combustor 7, is cooled in the cooler 8 to remove water gas component ( H ₂ O) 36, thereby forming a carbon dioxide (CO ₂₎ 35 high purity. This carbon dioxide is then fed in the required amount in the positive electrode of the fuel cell 6 through the plenum 12.

In this connection it should be noted that the carbon dioxide circulation is only required when the fuel cell in the molten carbonate (MCFC) is used as a fuel cell and is not required if other fuel cells are used.

5 shows a typical configuration of the basic units included in the fourth embodiment. The low-temperature gasification furnace 2 is a cylindrical fluidized-bed furnace having an internally circulating flow of the fluidized medium and the materials in the furnace are increased to diffuse within the furnace for thereby implementing a stable gasification. Gas containing no oxygen is supplied inside the central part of the furnace where the fluidized medium moves downwards and the gas containing oxygen is supplied to the furnace peripheral portion. This allows selective combustion of char formed in the low-temperature gasification furnace, contributing to an increase in carbon conversion rate and an increase in the cold gas efficiency. The high-temperature gasification furnace 15 is a furnace for burning cyclone type slagging.

The cylindrical fluidized-bed furnace shown in Figure 5, will be described in more detail. The conical distributor plate 106 is disposed at the bottom of a cylindrical fluidized-bed furnace. The fluidizing gas supplied through the distributor plate 106 includes a central fluidizing gas 207 which is fed into the furnace in a flow directed upward from the central portion 204 bottom, and a peripheral fluidizing gas 208 which is fed into the furnace in a flow directed upward from a peripheral portion of the bottom 203.

The central fluidizing gas 207 is a gas containing no oxygen, and the peripheral fluidizing gas 208 is an oxygen-containing gas. The total amount of oxygen in the whole fluidizing gas is set to 10% or more or 30% or less of the theoretical amount of oxygen required for combustion of combustible matter. Thus, the furnace 1 is maintained within a reducing atmosphere.

The relative oxygen content of 10 to 30% - this value in the case where the starting material used combustibles having a low calorific value, such as municipal wastes, and when the starting material used combustibles having a high calorific value, such as plastic waste, the relative oxygen content of from 5 to 10%.

The mass flow of the central fluidizing gas 207 should be set to a lower value than the mass flow rate of peripheral fluidizing gas 208. The upward flow of fluidizing gas to the upper peripheral region of the furnace is deflected toward a central region of the furnace through the deflector 206. Therefore, the movable layer is formed in the central region of the furnace 209, in which the fluidized medium (generally silica sand) moves downward and is scattered by the distributor plate. the fluidized bed 210 is formed in the peripheral region of the furnace where the fluidized medium is actively fluidized. As indicated by arrows 118, the fluidized medium which ascends into the fluidized bed 210 in the peripheral region of the furnace, is deflected baffle 206 in the upper part of the moving bed 209 and descends in the moving bed 209. Then, as indicated by arrows 112, the fluidized medium moves along the distributor plate 106 liquefying and the gas moves to the bottom of the fluidized bed 210. Thus, the fluidized medium circulates in the fluidized bed 210 and the moving bed 209 as indicated by arrows 118, 112.

When the material 21 fed into the top of the moving bed 209 through the dispenser 1 are lowered together with the fluidizing medium in the moving bed 209, the starting materials pass volatilize by heating the fluidizing medium. Since the movable layer 209 is absent or oxygen bit, the pyrolysis gas (produced gas) obtained by gasification, which contains the volatile materials not burned, and passes through the moving bed 209 as indicated by arrows 116. Consequently, the movable layer 209 forms a zone G gasification. The resulting gas moves in the "freeboard" portion 102 as shown by arrow 120, and is output from the gas release as a gas 108 g.

Charred material (fixed carbon) and tar produced in the moving bed 209, which is not gasified, move together with the fluidized medium from the lower portion of the movable layer 209 to the bottom of the fluidized bed 210 in the peripheral region of the furnace as indicated by arrows 112, and is partially oxidized for account peripheral fluidizing gas 208 having a relatively large oxygen concentration. Consequently, the fluidized bed 210 forms the oxidation zone S. In the fluidized bed 210, the fluidized medium is heated by the heat of combustion in a fluidized bed. Fluidized medium heated to a high temperature, the baffle 206 is deflected as indicated by arrows 118, and transferred into the moving bed 209 where it serves as a heat source for gasification. Thus, the fluidized bed is maintained at a temperature ranging from 400 to 1000 ° C, preferably from 400 to 600 ° C, thereby providing a continuous controlled flow of the combustion reaction. Annular outlet 205 is formed in the incombustibles peripheral portion gasification furnace bottom of a fluidized bed for 22 incombustible substances.

In accordance with the Figure 5 gasification furnace with the fluidized bed gasification zone G and the oxidation zone S are formed in the fluidised bed in two zones of the fluidized medium circulates. Because the fluidized medium serves as a medium transporting the heat in the gasification zone G is formed a combustible gas of good quality, having a high calorific value, and charred substance and resin, which are difficult gasified efficiently burned in the oxidation zone S. Consequently, the efficiency of gasifying combustible matter such as wastes, can be raised and can be generated product gas having a good quality. Such a gasification furnace with a fluidized bed is the most suitable low-temperature gasification furnace in the embodiments from the first to the third. The low-temperature gasification furnace is not limited to a cylindrical fluidized-bed furnace, and, as in the above embodiments may be used or kiln type furnace stoker type.

Fluidized bed furnace and the circulating flow, as shown in Figure 5, is more effective when as the fluidized medium of the fluidized bed particles are used to ensure the acceleration of reduction of molecular weight hydrocarbons, such as catalysts based on molybdenum or nickel-based catalysts, cobalt-molybdenum or alkali metals such as sodium or potassium, or a simple substance or in the form of a metal oxide, an alkaline earth metal such as calcium. The reason for this is as follows: when the molecular weight of hydrocarbons is reduced in the presence of catalyst particles in a reducing atmosphere, the deposition of the carbon bound to the catalyst surface and thus reduces the functional capability of the catalyst. However, in the case of a fluidized bed furnace, of the type with internal circulation flow in which there is within the oxidation zone furnace having a relatively high oxygen partial pressure, the carbon on the catalyst can be burned and removed in the oxidation zone. Because the catalyst particles again reduced catalytic activity due to the removal of carbon deposited on the surface of the particles, the effective utilization of the catalyst can be realized.

Next will be described in more detail incinerator slagging cyclone type. The high-temperature gasification furnace 15 includes a cylindrical primary gasification chamber 15a having a substantially vertical axis, a secondary gasification chamber 15b, which is slightly inclined in the horizontal direction, and a third gasification chamber 15c disposed downstream of the secondary gasification 15b chamber and having at a substantially vertical axis. The hole 142 for discharging the slag located between the secondary gasification chamber 15b and third chamber 15c gasification. Up to 142 holes for discharging slag contained most of the ash enters the slag and is discharged through an opening 142 for discharging slag. The resulting gas is fed to an incinerator slagging cyclone type in the tangential direction so that a swirling gas flow is generated inside the primary gasification chamber 15a. The produced gas supplied into the combustion furnace slagging cyclone type forms a swirling flow, and solid matter contained in the gas is trapped on the circumferential inner surface of the wall due to centrifugal force. Therefore, the percentage of slag formation and the percentage of slag capture high, and it is unlikely the scattering of slag mist.

Oxygen is fed into the combustion furnace slagging cyclone type via a plurality of nozzles 134 so as to properly maintain the temperature distribution in the furnace. The temperature distribution is regulated so that the decomposition of hydrocarbons and the formation of slag of fly ash was completed in the primary gasification chamber 15a and the secondary gasification chamber 15b. When applied, for example, one oxygen only, then there is a danger burning nozzle. Therefore, oxygen is diluted with steam or something similar before it is fed to the extent as required. Furthermore, water vapor contributes to the realization of the steam reforming of hydrocarbons to reduce the molecular weight and thus must be supplied in the required quantity. This is because the interior of the furnace has a high temperature, and when the amount of steam is insufficient, the condensation polymerisation to form graphite having a very low reactivity, which is the cause of the loss of unburnt fuel.

The slag flows down on the bottom surface of the secondary gasification chamber 15b and is discharged as molten slag 142 through the opening 26 for discharging slag. A third gasification chamber 15c serves as a buffer zone which prevents the cooling hole 142 for discharging of slag by radiation cooling from a waste heat boiler located downstream of the tertiary gasification chamber 15c, and serves to reduce the molecular weight of the gas is not decomposed. The outlet 144 for the output product gas made in the upper end of the tertiary gasification chamber 15c, and the radiation plate 148 is located at the bottom of the tertiary gasification chamber 15c. The radiation plate 148 is designed to reduce the amount of heat radiated through the outlet opening 144 by radiation. Numeral 132 denotes a "start" nozzle, and numeral 136 denotes a stabilizing nozzle. The organic material and the hydrocarbons contained in the produced gas are completely decomposed in the high-temperature gasification furnace into hydrogen, carbon monoxide, water vapor and carbon dioxide. The gas produced in the high-temperature gasification furnace 15 is discharged through the opening 144 to the exhaust gas, and then cooled to 650 ° C or below in a waste heat boiler 16, which is a radiation boiler for the solidification of molten salts of alkali metals. Alkali metal salts 24 after the solidification is then captured via the dust collector 3. The high-temperature gasification furnace is not limited to this type of furnace as the combustion furnace slagging cyclone type, and may be another type of a gasification furnace.

6 shows the structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to the fifth embodiment of the present invention. The fifth embodiment shown in Figure 6, is an embodiment in which the configuration of the high-temperature gasification furnace in a modified configuration which is preferred for the discharge of slag. Specifically, the high-temperature gasification furnace 15 has a furnace structure of a two-stage and lower-stage upper stage. The resulting gas is fed to the furnace top stage high-temperature gasification furnace 15 and flows toward the lower-stage furnace. In this case, the gas flows in the direction in which the slag is lowered by gravity. Thus, the flow is smooth and unlikely to cause problems associated with plugging the holes for the output of slag. HRSG representing a radiation boiler 16 is mounted on the side of the high-temperature gasification furnace bottom stage 15. The rest of the structure is the same as in the fourth embodiment shown in Figure 4.

7 shows a structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to a sixth embodiment of the present invention. The sixth embodiment shown in Figure 7, is the same as the fourth embodiment shown in Figure 4, except that the sixth embodiment relates to a pressurized system. More specifically, the low-temperature gasification furnace 2, the high-temperature gasification furnace 15, the dust collector 3, the device 4 for trapping corrosive gases, the fuel cell 6, the gas combustor 7 and 8 the gas cooler 13 placed in a high pressure vessel. Inside of the tank apparatus 13 is placed under increased pressure, the pressure is increased to a predetermined value. As in the third embodiment shown in Figure 3, this embodiment is a system that can implement three stage power generation in combined cycle: a fuel cell power generation, power generation gas turbine and steam turbine power generation.

When the starting material combustible plastic materials are used among plastic waste having a high content of chlorine, such as PVC, special attention should be paid to the removal of chlorine. 8 shows the structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to a seventh embodiment of the present invention. In this embodiment, the produced gas containing solids such as char derived from the top of the low-temperature gasification furnace 2 is supplied to the high-temperature gasification furnace 15, and, entering into contact with oxygen and water vapor contained in the gasifying agent, the produced gas is fully gasified in high temperature of 1300 ° C or higher. Ash contained in the gas is converted into slag mist due to high temperature, and slag mist with produced gas coming in the cooling chamber 15A. The cooling chamber 15A gidropulpiruetsya slag 26 in the water and discharged to the outside of the system. On the other hand, the resulting gas, which entered the cooling chamber 15A, 15A in a water-cooled cooling chamber, and the chlorine contained in the produced gas is derived by washing the gas with water. The purified product gas from which chlorine is removed is supplied to the fuel cell 6, and is used to generate electricity. The exhaust gas discharged from the negative electrode side of the fuel cell 6, is supplied by the blower 9 high low-temperature gasification furnace 2 through the gas combustor 7, and is reused as a gasifying agent and a fluidizing gas into the low-temperature gasification furnace 2.

On the other hand, exhaust gas discharged from the positive electrode side of the fuel cell 6, together with the exhaust gas discharged from the gas combustion chamber 7 is supplied to the gas turbine 14, where power is generated. The exhaust gas discharged from the gas turbine 14 is discharged through a waste heat boiler 10 to the outside of the system.

9 shows the structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to an eighth embodiment of the present invention. The eighth embodiment shown in Figure 9 represents a variant in which the present inventors proposed a combined gasification furnace which is used as the low-temperature gasification furnace. This furnace comprises a gasification chamber, the char combustion chamber and the heat recovery chamber integrated in one furnace. As shown in Figure 9, in the low-temperature gasification furnace 2 is divided by a first partition wall 302 on the section 303 and the gasification section 304 incineration. The first partition wall 302 is provided with a communication hole 337 for connecting the gasification section 303 and the combustion section 304 with each other. In the gasification section of the gasification chamber 303 is 305. Hole 349 is for withdrawal of gas in the gasification section 303, and the resulting gas is withdrawn through the opening 349 to the outside of the gas outlet of the furnace.

On the other hand, the combustion section 304 is further divided by a second partition wall 350 in combustion chamber 306 and charred materials heat recovery chamber 307. However, the upper part of the combustion section 304 is not divided, and the combustion chamber char and the heat recovery chamber are combined in the "freeboard" part. Appropriate exhaust gases are mixed together in the "freeboard" part, and then output through the output opening 351 of the gas out of the furnace. The camera 307 mounted heat recovery heat exchanger surface 346, and the heat can be taken from the fluid medium. Lower coupling hole 340 holds the second partition wall 350, and a lower connection hole 340 moves the fluidized medium 306 between the chamber and the char combustion chamber 307 in view of the heat recovery area of ​​the top open. Fluidizing gas is supplied so that in the gasification chamber 305 formed within the fluidized bed, two different region of the fluidized bed. The result is a circulatory flow that the fluidised medium moves downward in a weakly fluidized region layer and moves upward in a strongly fluidized region layer.

On the other hand, in the combustion section 304 and the fluidizing gas is supplied so that combustion chamber 306 within the fluidized char layer formed two different areas of the fluidized bed. The result is a circulatory flow that the fluidised medium moves downward in a weakly fluidized region layer and moves upward in a strongly fluidized region layer. Further, the heat recovery chamber 307, moreover, is injected fluidizing gas so as to provide a substantially small superficial gas velocity, and thus weakly The liquefied area as a downward flow of the fluidized medium is formed over the furnace bottom.

Starting material 21 is introduced into the gasification chamber 305 in the low-temperature gasification furnace 2 operated under pressure, where the starting material 21. The pyrolysis gas produced in the gasification chamber 305 is introduced into the high-temperature gasification furnace 15. Additional char produced in the gasification chamber 305, charred particles having a size such that the charred particles will remain within the fluidized bed, they are transported in the flow of the fluidized medium 306 char combustion chamber substances where these charred particles are completely burnt. Combustion air is fed into the chamber 306 for burning the char and gas resulting from combustion with the exhaust gas discharged from the positive electrode of the fuel cell 6 is fed to the gas turbine 14 for power generation. Среди обуглившихся веществ, полученных в камере 305 газификации, обуглившиеся частицы, имеющие такой размер, что такие частицы будут уноситься с потоком полученного газа в высокотемпературную газификационную печь 15, они будут взаимодействовать с кислородом и водяным паром при высокой температуре 1300°С или выше для осуществления полной газификации. Отработавший газ, выведенный со стороны отрицательного электрода топливного элемента 6, сжимается с помощью высокотемпературного нагнетателя 9, а остаточное топливо полностью сжигается в газовой камере 7 сгорания. Газ, полученный в результате сжигания, который затем повторно используется в качестве газифицирующего агента и сжижающего газа в камере 305 газификации низкотемпературной газификационной печи 2, и, кроме того, он используется в качестве разжижающего газа для разжижения кислорода, чтобы его подавать в высокотемпературную газификационную печь 15. Поскольку отработавший газ, выведенный со стороны отрицательного электрода, имеет температуру примерно 700°С, то подача кислорода с целью обеспечения тепла для газификации в камере 305 газификации низкотемпературной газификационной печи 2 может быть значительно уменьшена для достижения высокой эффективности холодного газа.

Комбинированная газификационная печь, показанная на фиг.9, более эффективна, когда в качестве псевдоожиженной среды псевдоожиженного слоя используются частицы, обеспечивающие функцию ускорения снижения молекулярной массы углеводородов, такие как катализаторы на основе никель-молибден или на основе кобальт-молибден, или щелочные металлы, такие как натрий или калий, или в виде простого вещества или в форме оксида металла щелочноземельные металлы, такие как кальций. Причина этого следующая. Когда молекулярная масса углеводородов уменьшается в присутствии частиц катализатора в восстановительной атмосфере, то происходит осаждение угля на поверхность катализатора и неизбежно понижение функциональной способности катализатора. Однако в случае комбинированной газификационной печи, в которой секция газификации и секция сжигания явно разделены друг от друга и находятся в одной и той же печи, а псевдоожиженная среда циркулирует через секцию газификации и секцию сжигания, по сравнению с печью с псевдоожиженным слоем и с циркулирующим внутри потоком, показанной на фиг.5, углерод, осажденный на поверхности катализатора, может более надежно сжигаться и удаляться в секции сжигания. Поэтому частицы катализатора восстанавливают свою каталитическую активность опять до высокого уровня вследствие удаления углерода, осажденного на поверхности частиц, в более высокой степени. Таким образом, может быть реализовано значительно более эффективное использование катализатора.

Отработавший газ, выведенный со стороны положительного электрода топливного элемента 6, и имеет высокую температуру и содержит кислород и, таким образом, может быть эффективно использован в качестве сжижающего газа, выполняющего такую же функцию, как и газ сжигания в камере 306 сжигания обуглившихся веществ в низкотемпературной газификационной камере 2. Когда рабочее давление низкотемпературной газификационной печи выше, чем рабочее давление топливного элемента, тогда давление отработавшего газа должно быть повышено с помощью высокотемпературного нагнетателя до подачи отработавшего газа в низкотемпературную газификационную печь. С другой стороны, когда рабочее давление топливного элемента достаточно высокое по сравнению с давлением в низкотемпературной газификационной печи, тогда давление отработавшего газа из топливного элемента может с выгодой использоваться само по себе. Если необходимо, то при вводе отработавшего газа, выведенного из секции 304 сжигания в комбинированной газификационной печи, в газовую турбину 14 пыль, содержащаяся в газе, может быть удалена с помощью пылеуловителя, такого как циклонный пылеуловитель, или с помощью керамического фильтра.

Более того, нет необходимости, чтобы температура камеры 305 газификации поддерживалась за счет использования теплосодержания путем циркуляции псевдоожиженной среды между камерой 306 сжигания обуглившихся веществ и камерой 305 газификации. Поэтому "время жизни" обуглившихся веществ, циркулирующих вместе с псевдоожиженной средой внутри камеры газификации, может по желанию регулироваться, и, следовательно, различные горючие вещества, имеющие различное содержание связанного углерода, которые трудно газифицировать, могут быть использованы в качестве топлива. Остальная часть структуры настоящего варианта такая же, как в седьмом варианте, показанном на фиг.8.

На фиг.10 показана структура системы, вырабатывающей электрическую энергию, с топливным элементом и с комбинированным циклом, соответствующая девятому варианту осуществления настоящего изобретения. Как и в варианте, показанном на фиг.9, девятый вариант осуществления настоящего изобретения, показанный на фиг.10, представляет собой вариант, в котором комбинированная газификационная печь, содержащая камеру газификации, камеру сжигания обуглившихся веществ и камеру рекуперации тепла, объединенные в одной печи, применяется в качестве низкотемпературной газификационной печи, соответствующей настоящему изобретению. В настоящем варианте, как и в варианте, показанном на фиг.9, камера 305 газификации, камера 306 сжигания обуглившихся веществ и камера 307 рекуперации тепла размещены в низкотемпературной газификационной печи 2. В настоящем варианте исходный материал 21 подается в камеру 305 газификации в низкотемпературной газификационной печи 2, работающей при атмосферном давлении, и все обуглившиеся вещества, полученные в камере 305 газификации, подаются в камеру 306 сжигания обуглившихся веществ, где происходит сжигание обуглившихся веществ. Отходящий газ, выведенный из камеры 306 сжигания обуглившихся веществ, вместе с отработавшим газом, выведенным со стороны положительного электрода топливного элемента 6, подается в котел-утилизатор 10 для рекуперации тепла. Газ, полученный в камере 305 газификации, пропускается через пылеуловитель 3 и аппарат 4 для удаления агрессивных газов и затем вводится в устройство 5 для риформинга топлива, топливный элемент 6 и газовую камеру 7 сгорания, в этом порядке; аппараты и устройства выполнены в объединенном виде. При рассмотрении отработавшего газа, выведенного со стороны отрицательного электрода топливного элемента 6, остаточное топливо полностью сжигается в газовой камере 7 сгорания. Газ, полученный в результате сжигания, затем повторно используется в качестве газифицирующего агента и сжижающего газа для камеры 305 газификации в низкотемпературной газификационной печи 2. Отходящий газ, выведенный из котла-утилизатора 10, с помощью нагнетателя 11 подается в пылеуловитель 18, где содержащаяся зола удаляется из отходящего газа и затем выводится. Остальная структура такая же, как в варианте, показанном на фиг.2.

На фиг.13 показана структура системы, вырабатывающей электрическую энергию, с топливным элементом и с комбинированным циклом, соответствующая десятому варианту осуществления настоящего изобретения. Десятый вариант, показанный на фиг.13, представляет собой вариант, в котором отработавший газ, выведенный со стороны отрицательного электрода топливного элемента, не циркулирует. То есть настоящий вариант представляет собой такой же вариант, как система, соответствующая первому варианту, показанному на фиг.1, за исключением того, что устранен канал, через который отработавший газ, выведенный со стороны отрицательного электрода топливного элемента 6, возвращается в низкотемпературную газификационную печь 2. Поэтому отработавший газ, выведенный со стороны отрицательного электрода топливного элемента 6, подается только в газовую камеру 7 сгорания и в устройство 5 для риформинга топлива. В качестве газифицирующего агента, подаваемого в псевдоожиженный слой, может использоваться воздух, кислород, водяной пар и их комбинация. Остальная часть структуры такая же, как в варианте, показанном на фиг.1.

В вариантах осуществления изобретения, показанных на фиг.1-13, в качестве примеров топливного элемента описан топливный элемент с расплавленным карбонатом (ТЭРК). Настоящее изобретение применимо, конечно, и и для топливного элемента с твердым электролитом (ТЭТЭ). Более того, при добавлении процесса конверсии СО для преобразования СО и Н ₂ O, содержащихся в полученном газе, в Н ₂ и CO ₂ , чтобы тем самым удалить СО, возможно применять настоящее изобретение для топливного элемента с фосфорной кислотой и топливного элемента с полимерным электролитом. Далее, и положительно влияет на работу системы, если только водород, содержащийся в полученном газе, селективно отделяется с помощью мембраны, для которой проницаемым является только водород, или с помощью сплава, сорбирующего водород, для выработки электрической энергии в топливном элементе с фосфорной кислотой (ТЭФК) или топливном элементе с полимерным электролитом (ТЭПЭ).

На фиг.14 показана структура системы, вырабатывающей электрическую энергию, с топливным элементом и с комбинированным циклом, соответствующей одиннадцатому варианту осуществления настоящего изобретения. Одиннадцатый вариант, показанный на фиг.14, представляет собой типичный вариант осуществления настоящего изобретения, в котором добавлен процесс конверсии СО. А более конкретно, конвертер 17 для конверсии СО размещен ниже по потоку от устройства 5 для риформинга топлива, так что может осуществляться конверсия СО. Следовательно, в качестве топливного газа в топливный элемент 6 может подаваться только водород. В случае, когда имеется проблема, связанная с утечкой СО в технологическом процессе конверсии СО, после процесса конверсии СО может быть предусмотрен процесс удаления СО. СО может удаляться с помощью водородпроницаемой мембраны, для которой только водород является селективно проницаемым, или в альтернативном варианте с помощью сплава, сорбирующего водород, который может селективно сорбировать только водород. Остальная часть структуры системы такая же, как в системе, показанной на фиг.1.

15 shows a structure of the system, generating electricity, with the fuel cell combined-cycle corresponding to a twelfth embodiment of the present invention. The twelfth embodiment shown in Figure 15, is a typical embodiment of the present invention, wherein the process is provided after the CO conversion process of hydrogen release using the hydrogen absorbing alloy. According to this embodiment, the converter 17 for conversion of CO is placed downstream of the device for the fuel reformer 5 so that it was possible to carry out the conversion of CO. Furthermore, the alloy 19 sorbing hydrogen, positioned downstream of the converter 17 for CO conversion. Alloy 19 sorbing hydrogen, can absorb and store hydrogen in an amount of 1,000 times the volume of the hydrogen absorbing alloy. Thus, a buffer from the hydrogen absorbing alloy having an adequate capacity for the hydrogen accumulation, and it can contribute to the gasification furnace operation regardless of load power generation by the fuel cell. This can greatly increase the degree of freedom for the use in the whole system. The working temperature of the alloy absorbing hydrogen on a lanthanum or other rare earth metals, that are currently being developed, about 100 ° C. Therefore, if necessary, upstream of the hydrogen absorbing alloy, a cooler may be installed. Водород, полученный с помощью сплава 19, сорбирующего водород, подается в топливный элемент 6, а остаточный газ соединяется с отработавшим газом, выводимым со стороны отрицательного электрода топливного элемента 6. Вместо сплава, сорбирующего водород, может быть размещен резервуар с газом. А конкретно, сплав, сорбирующий водород, или резервуар с газом могут быть предусмотрены как средство для регулирования уровня нагрузки газификационной печи, чтобы подавать водород в топливный элемент 6 в соответствии с нагрузкой выработки энергии, тем самым производя выработку энергии в количестве, которое может покрывать потребность в электрической энергии. Поскольку сплав, сорбирующий водород, имеет функцию селективного поглощения водорода, то, если количество СО, содержащегося в полученном газе, чуть, конвертер 17 для конверсии СО может не устанавливаться.

Squeeze starting materials formed in the apparatus 1 to download the source material is introduced into the dryer 30 where the squeeze of raw materials is heated, vaporized and dried by the steam produced in the boiler 10 and / or boiler 16. The exhaust steam released from the squeeze of raw materials , has an unpleasant odor and, therefore, it is mixed with high-temperature gas in the boiler 10 and / or the boiler 16 for odor removal. Although the squeeze of raw materials can be mixed directly with the high temperature gas in the boiler 10 and / or the boiler 16 without drying with by drying, but it is assumed that, as compared with direct blowing squeeze of raw materials in the heat recovery process is more advantageous implementation of the evaporation and drying pomace raw materials out of the system, after which the process in the heat recovery process applied only vapor effluent obtained because the magnitude of reduction of the gas temperature is so small that the quantity of steam formed in the process of heat recovery can be increased. Namely, as in this embodiment, when the high-temperature gasification furnace operated at a temperature of 1000-1500 ° C is used in the gasification process and the process of heat recovery process is carried out downstream of the high-temperature gasification furnace, such structure is very advantageous. Due to the fact that the temperature of the produced gas introduced into the heat recovery process is high, about 1300 ° C, heat transfer in the heat recovery process is performed by heat transfer by radiation and, therefore, achieved a greater degree of increasing the amount of recovered heat while maintaining the gas at a high temperature.

In the embodiments shown in fig.1-22, are exemplary combinations of various apparatus used in manufacturing processes of gasification to power generation in the fuel cell. and other combinations of devices other than the exemplary, which utilize apparatuses shown in fig.1-22.

As understood from the above description, according to the present invention, combustibles are gasified to produce gas and the produced gas is then used in a chemical reaction to generate electricity with high efficiency.

Furthermore, according to the present invention, the gas produced in the gasification furnace is supplied to the apparatus for generating energy to produce electrical energy, and an exhaust gas containing a large amount of steam after the energy production is reused as a gasifying agent in the low-temperature gasification furnace. Thus, reuse of the heat content of the exhaust gas as a heat source for gasification can reduce the required amount of combustible part of flammable substances and to increase the gasification efficiency. Moreover, the exhaust gas containing a large amount of water vapor can contribute to the acceleration of the gasification reaction by the effect of steam reforming, which can increase the effect of gasification.

Furthermore, according to the present invention, combustibles such as combustible wastes or coal stably gasified in the low-temperature gasification furnace to produce gas, the toxic components of the fuel cell is removed from the product gas and then the purified gas is introduced into the fuel cell to generate electricity with high efficiency .

Industrial Applicability

The present invention relates to a power conversion technology for converting chemical energy of combustibles to electric energy with high efficiency. The present invention may be used in the system, generating electricity, in which combustibles such as combustible wastes or coal are gasified to produce gas, and the produced gas is then used as fuel gas in the fuel cell to generate electrical energy.

CLAIM

1. Apparatus for reforming a gas containing a furnace to a fluidized bed gasification, a gasification chamber having a combustion chamber and charred materials feeder combustibles in the gasification furnace and the fluidizing gas feeding device for supplying a fluidizing gas into the gasification furnace, with combustibles are gasified in the furnace for the gasification to produce gas and char, and the produced gas is reformed by using a catalyst for producing a reformed gas in the chamber for the gasification, wherein said catalyst is restored using the combustion of this char in the combustion chamber carbonized substances, and reduced the catalyst is reused in the gasification chamber.

2. A system that produces electrical energy by gasification of combustibles, comprising a furnace for the gasification of combustibles to produce gas, a fuel cell for generating electric power using the produced gas supplied from the gasification furnace, with the exhaust gas discharged from the fuel cell, fed into a gasification furnace for use in the exhaust gas as a gasifying agent to the gasification furnace.

3. The system of claim 2, wherein the furnace is a gasification furnace to the fluidized-bed gasification and gasifying agent is used as a fluidizing gas.

4. The system of claim 2 or 3, wherein the exhaust gas which is derived from the negative electrode of the fuel cell is introduced to the gasification furnace as a gasifying agent.

5. The system of claim 4, wherein the gasification furnace has a gasification chamber and the char combustion chamber, and the exhaust gas, which is derived from the negative electrode of the fuel cell is introduced into the gasification chamber as a gasifying agent.

6. The system of claim 5, wherein the exhaust gas which is withdrawn from the positive electrode of the fuel cell is introduced into the char combustion chamber substances.

7. A system that produces electrical energy by gasification of combustibles, comprising a furnace for the gasification of combustibles to produce gas, high-temperature gasification furnace for reforming the resulting gas to produce a reformed gas, a fuel cell for generating electric power using the produced gas supplied from the furnace gasification, wherein the exhaust gas discharged from the fuel cell is supplied to the at least one oven: or furnace for gasification or furnace for high temperature gasification to use the exhaust gas as a gasifying agent for at least one furnace: or gasification furnaces, or for high-temperature gasification furnace.

8. The system of claim 7, wherein the furnace is a gasification furnace to the fluidized-bed gasification and gasifying agent is used as a fluidizing gas.

9. The system of claim 7 or 8, wherein the exhaust gas, which is derived from the negative electrode of the fuel cell is introduced in at least one furnace: furnace or gasification unit, or to a high-temperature gasification furnace as a gasifying agent.

10. The system of claim 9, wherein the gasification furnace has a gasification chamber and the char combustion chamber, and the exhaust gas, which is derived from the negative electrode of the fuel cell is introduced into the gasification chamber as a gasifying agent.

11. The system of claim 10, wherein the exhaust gas, which is derived from the positive electrode of the fuel cell is introduced into the char combustion chamber substances.

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Publication date 16.02.2007gg

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