Desulfurization apparatus

Abstract: The speed of a desulfurization reaction and the regeneration reaction and reaction rate of each of the reactions are improved and a total size of an apparatus can be made compact. A desulfurization apparatus comprises a sulfide ion producing portion (54) which react with a sulfur compound being supplied, and produce a sulfide ion, sulfur compound supply portion (52) supplying a gas containing the sulfur compound to the sulfide ion producing portion (54), and a sulfur compound discharge portion (53) discharging the sulfur compound produced by a reaction with the sulfide ion from the sulfide ion producing portion (54). Since the structure is made in the above manner, the sulfur contained in the gas supplied from the sulfur compound supply portion (52) is condensed in the gas flowing through the sulfur compound discharge portion (53), so that the sulfur can be efficiently recovered.

Description: BACKGROUND OF THE INVENTION FIELD OF THE INVENTION The present invention relates to a desulfurization apparatus for performing a desulfurization of a crude gas containing a sulfur such as a coal gasification gas under a high temperature. DESCRIPTION OF THE RELATED ART Among a fossil fuel coal is distributed widely in the world in comparison with oil and natural gas. Fossil fuel reserves are plentiful and are expected to be used as a future fuel for generating electric power. A known method of generating electric power using a coal as a fuel is pulverized coal thermal power in which coal is pulverized in order to be burned. However, in view of a thermal efficiency and adaptability to the environment, there has been developed a coal gasification compound electric power plant in which coal is gasified. The gasified coal undergoes desulfurization and is burned. The burned gas is then fed to a gas turbine and a steam turbine to generate electric power. Fig. 1 is a block diagram of a coal gasification combined electric power plant using a desulfurization apparatus. A coal gasification compound electric power plant 21 has coal gasification equipment 22, gas purification equipment 41, and compound electric power generating equipment 24. The coal gasification equipment 22 includes gasification furnaces 27a and 27b,that mix pulverized coal 25 and a gasification agent 26 (normally, oxygen) and perform gasification under a predetermined condition. A gas cooler 28 cools coal gas 11 exhausted from the gasification furnace 27b. The coal gas 11 exhausted from the gas cooler 28 passes through the desulfurization tower 2 within the dry desulfurization apparatus 1. Thereafter, the gas 11 passes through a filter 29 provided within the scrubbing apparatus 23. Then, the gas 11 is supplied to the combined electric power generating equipment 24. The coal gas 11 is burned in a burner 30 provided within the combined electric power generating equipment 24. The burned gas is supplied to an exhaust heat recovery boiler 33 through a gas turbine 31. A condenser 36 and a steam turbine 35 are provided in the exhaust heat recovery boiler 33. An operation of the coal gasification combined electric power plant 21 having the above structure will be described below. The pulverized coal 25 and the gasification agent 26 are mixed. The mixed gas is supplied to the gasification furnace 27a which has a high temperature. In the gasification furnace 27a, a reaction in which carbon is mainly oxidized so as to produce carbon dioxide is taken effect. An inner portion of the gasification furnace 27b is under high pressure and a reduction reaction takes effect mainly between the carbon dioxide a carbon therein. A carbon oxide is produced through the reduction reaction. Accordingly, the gasification furnaces 27a and 27b gasify the coal at a high temperature and a high pressure (which varies according to the gasification method, for example, about 1400 (C and about 2 MPa) so as to produce the coal gas 11. The produced coal gas 11 is composed of carbon oxide, hydrogen, carbon dioxide, and water vapor. The coal gas 11 is cooled to a suitable temperature (about 500 (C) in the gas cooler 28. The cooled coal gas 11 is fed to the desulfurization tower 2 within the gas purification equipment 41. The desulfurization tower 2 removes H2S contained in the coal gas 11. The coal gas 11 exhausted from the desulfurization tower 2 passes through the filter 29 thereafter. The filter 29 removes dust contained in the coal gas 11 at the time the coal gas 11 passes therethrough. Accordingly, the desulfurization tower 2 and the filter 29 remove sulfur and fine particle that cause corrosion and abrasion of the gas turbine by passing the coal gas 11 therethrough. The clean coal gas 11 from which sulfur and fine particles are removed is supplied to the combined electric power generating equipment 24. The clean coal gas 11, purified in the gas purification equipment 41, is burned in the burner 30. The burned combustion gas rotates the gas turbine 31 to generate electric power. An exhaust gas 32 exhausted from the gas turbine 31 is fed to the exhaust heat recovery boiler 33. The exhaust heat recovery boiler 33 takes the heat from the exhaust gas 32 so as to produce steam 34. The produced steam 34 rotates the steam turbine 35 to generate electric power. The steam 34, exhausted from the steam turbine 35, is condensed in the condenser 36. A part of the condensed steam is fed back to the exhaust heat recovery boiler 33. The remainder of the condensed steam is fed to the gas cooler 28. Further, heat recovered from the coal gas 11 in the gas cooler 28 is combined with the steam 34 fed from the condenser 36. This recovered heat and the steam 34 fed from the exhaust heat recovery boiler 33 are both fed to the steam turbine 35. Thereafter, the steam 34 is discharged from the steam turbine 35 and returned to the gas cooler 28 through the condenser 36. When coal as a raw material for the coal gasification compound electric power plant 21 having the above structure is gasified, most of the sulfur contained in the coal becomes a hydrogen sulfide and is mixed with the coal gas 11. As a desulfurization apparatus for removing the hydrogen sulfide at a high temperature, the dry desulfurization apparatus 1, which uses an iron oxide as a desulfurization agent, is used. The dry desulfurization apparatus 1 performs the desulfurization while keeping a temperature of the coal gas 11 containing hydrogen sulfide produced in the gasification furnaces 27a and 27b high without decreasing the temperature for, as long as possible. The fluid that performs the desulfurization is supplied to the compound electric power generating equipment 24. Further, the dry desulfurization method exhibits excellent thermal efficiency. A structure of the dry desulfurization apparatus 1 will be described below with reference to Fig. 2. The dry desulfurization apparatus 1 comprises a desulfurization tower 2, a regeneration tower 3, a reduction tower 37, a sulfur condenser 8, a circulation gas compressor 9 and a heater 10. The coal gas 11 flows from an end (the lower portion in the drawing) to the desulfurization tower 2. The flowing coal gas 11 is brought into mixture with a desulfurization agent 38 provided within the desulfurization tower 2. A chemical reaction between the coal gas 11 and the desulfurization agent 38 occurs according to the following formula (1). Fe2O3 + 2H2S + H2 → 2FeS + 3H2O The coal gas 11 from which the sulfur is removed thereafter flows out from the other end (the upper portion in the drawing) of the desulfurization tower 2. The desulfurization agent 38 which absorbs the sulfur contained in the coal gas 11, thus becoming a sulfide, is fed to an end (the upper end in the drawing) of the regeneration tower 3. An air 39,includings oxygen, is supplied from the other end (the lower portion in the drawing) of the regeneration tower 3. A chemical reaction shown in the following formula (2) occurs between the sulfide and the air within the regeneration tower 3, so that the sulfide is oxidized. The sulfide can be regenerated by this oxidizing reaction. 4FeS+7O2 → 2Fe2O3 + 4SO2 The regenerated desulfurization agent 38 is again fed to the desulfurization tower 2 and reused. The desulfurization agent 38 is moved between the desulfurization tower 2 and the regeneration tower 3 by an air current transmission. The sulfur removed from the desulfurization agent 38 becomes sulfurous acid gas in the regeneration tower 3 that gas is then fed to the reduction tower 37 as a regeneration tower outlet gas 14. The regeneration tower outlet gas 14 supplied to an end (the lower portion in the drawing) of the reduction tower 37 undergoes a chemical reaction (3) with a smokeless coal 40 supplied from the other end (the upper portion in the drawing) of the reduction tower 37, as shown in the following formula: 2C + 2SO2 → 2CO2 + S2 A sulfur steam produced by the chemical reaction that flows into the sulfur condenser 8 (the upper portion in the drawing). The sulfur steam is cooled within the sulfur condenser 8. The sulfur steam condensed by the cooling is discharged to an outer portion of the dry desulfurization apparatus 1 as the chemical element sulfur 16. The tail gas 17 that flows from the other end (the lower portion in the drawing) of the sulfur condenser 8 is fed to the circulation compressor 9 and the pressure thereof increases. The tail gas 17 discharged from the circulation compressor 9 is fed to the heater 10 and the temperature thereof increases. A portion of the heated tail gas 17 is mixed with the coal gas 11 supplied to the desulfurization tower 2 and is then fed to the desulfurization tower 2. The remaining tail gas 13 is mixed with air 39 for regeneration and is then fed to the regeneration tower 3. However, in the conventional desulfurization apparatus mentioned above and the electric power plant using the same, the following problem has occurred. Since the desulfurization reaction or the regeneration reaction in the desulfurization tower 2 or the regeneration tower 3 is a solid-to-gas reaction, the reaction speed is less than that of a wet desulfurization apparatus. Further, a reaction rate of each of the chemical reactions is low. Accordingly, the amount of desulfurization agent 38 required in the desulfurization tower 2 or the regeneration tower 3 becomes large. Consequently, the size of the desulfurization tower 2 and the regeneration tower 3 must be large in comparison with that required in the wet desulfurization apparatus. As a result, the cost therefor increases. Further, the circulation amount of the desulfurization agent 38 increases and the power required for the air current transmission equipment of the desulfurization agent 38 and the electric power plant increases. As a result, the total size of the compound electric power plant using the conventional dry desulfurization apparatus increases. In addition, the power consumed within the electric power plant increases. WO 92/20431 which forms the preamble of claim 1 discloses a hydrogen sulfide membrane assembly, an acid gas membrane assembly, and, optionally, a dehydration membrane assembly. The membrane may be plate shaped and is capable of diffusing sulfide ion from sulfur containing gas. The sulfur containing gas is supplied to the membrane in a supply manifold whereas the sulfur discharge gas is recovered by a recovery manifold. SUMMARY OF THE INVENTION An object of the present invention is to provide a compact and inexpensive desulfurization apparatus, allowing efficient recovery of the sulfide. This object is solved by a desulurization apparatus comprising the features of claim 1. A preferred embodiment is defined in claim 2. There is provided a desulfurization apparatus comprising a sulfide ion producing portion reacting with a sulfur compound and producing a sulfide ion; sulfur compound supply portion disposed in one end of the sulfide ion producing portion and supplying the sulfur compound to the sulfide ion producing portion; and a sulfur compound discharge portion disposed at the other end of the sulfide ion producing portion that discharges the sulfur compound produced by a reaction with the sulfide ion from the sulfide ion producing portion. A plurality of the sulfur compound supply portions and a plurality of the sulfur compound discharge portions are alternately disposed through the sulfide ion producing portion, and the flow direction of the fluid within the sulfur compound supply portion is different from the flow direction of the fluid within the sulfur compound discharge portion. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a block diagram of an electric power plant using a conventional desulfurization apparatus; Fig. 2 is a block diagram of the conventional desulfurization apparatus; Fig. 3 is a perspective view of an embodiment of a desulfurization apparatus not within the scope of the invention; Fig. 4 is a block diagram of an electric power plant using the desulfurization apparatus; Fig. 5 is a perspective view of another embodiment of a desulfurization apparatus not within the scope of the invention; Figs. 6(a) and 6(b) are a front elevational view and a cross sectional view of an embodiment of a desulfurization apparatus in accordance with the invention; and Fig. 7 is a perspective view of an embodiment of a desulfurization apparatus not within the scope of the invention. DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of the desulfurization apparatus will be described below with reference to the drawings. Fig. 3 is a perspective view of a desulfurization apparatus of a first embodiment not within the scope of the invention. Fig. 4 is an electric power generating system using the desulfurization apparatus. The coal gasification compound electric power plant 6 1 (Fig.4) (an electric power generating system) using the desulfurization apparatus 51 has as its major components the coal gasification equipment 22, the desulfurization apparatus 51, a scrubbing apparatus 23, and a compound electric power generating equipment 24 (an electric power generating apparatus). In the coal gasification equipment 22, at first, coal 25 is supplied to a gasification furnace 27a having a high temperature together with a gasification agent (oxygen) 26 and they are mixed. The mixed coal and gasification agent 26 are gasified within the gasification furnace 27a at a high temperature and pressure (which varies in accordance with the gasification method; however, one example is an internal temperature of about 1400 C(degree) and an internal pressure of about2 Mpa. The produced coal gas 11 is mainly carbon oxide, hydrogen, carbon dioxide, and water vapor, and normally contains hydrogen sulfide of less than 1%. The coal gas 11 is cooled to a suitable temperature (about 700 (C) in a gas cooler 28. In the cooled coal gas 55, solid material is removed by a filter 62. Thereafter, the coal gas 55 is introduced into the flowing passage 52 in order to be processed in the desulfurization apparatus 51. The desulfurization apparatus 51 is structured such that a flowing passage 52 through which the gas flows in order to be to be processed (the sulfur compound supply portion) is disposed atone end of the sulfur moving body 54 having a planar plate shape (a sulfide ion producing portion) and a sulfur discharge gas flowing passage 53 (a sulfur compound discharge portion) is disposed at the other end thereof. The sulfur moving body 54 (which can be considered as an example of sulfuide ion producing portion ) in the desulfurization apparatus 51 is shaped as a planar having a thickness of about 1 mm. In this embodiment, the sulfur moving body 54 includes a molten carbonate such as a sulfur dissolved medium impregnated into a porous member to which a ceramic such as a lithium aluminate is sintered. For a carbonate, one of or a mixture of carbonates of alkali metals such as Li, Na and K, or a mixture of the alkali metal carbonate and a carbonate of an alkaline earth element such as Mg, Ca, Sr and Ba is used. When the carbonate is melted at a predetermined temperature (ranging from, for example, 400 C(degrees) to 850 C(degrees), there is a lot of carbonate ion CO32- within the solution. Hydrogen sulfide H2S contained in the coal gas 55 flowing through the flowing passage 52 in order to be processed is melted into the molten carbonate. Thereafter, a chemical reaction, as shown by the following formula (4), occurs taken with respect to the carbonate ion. H2S + CO32- → H2O + CO2 + S2- The sulfide ion produced by the chemical reaction of the formula (4) diffuses through the thickness of the sulfur moving body 54 within the molten carbonate. The diffused sulfide ion reaches an interface with respect to the sulfur discharge gas 56 flowing through the sulfur discharge gas passage 53 arranged in the back of the sulfur moving body 54. The sulfur discharge gas 56 is mainly composed of H2O and CO2. The flow of the sulfur discharge gas 56 is different from the flow of the coal gas 55. Concretely speaking, they flow opposite to each other. Accordingly, in the interface between the molten carbonate and the sulfur discharge gas 56, a chemical reaction, as shown in the following formula (5), which operates in the reverse direction of the formula (4) occurs. H2S + CO32- ← H2O + CO2 + S2- The produced hydrogen sulfide (a gas phase) is mixed into the sulfur discharge gas 56. At this time, when the product of the partial pressure of H2O and the partial pressure of CO2 contained in the sulfur discharge gas 56 is larger than the product of the partial pressure of H2O and the partial pressure of CO2 contained in the coal gas 55, the chemical reaction shown in the formula (5) is promoted. Further, the coal gas 55 from which sulfur is removed in the desulfurization apparatus 51 is scrubbed by the scrubbing apparatus 23. The scrubbed coal gas 55 is supplied to the combined electric power equipment 24. The coal gas 55 supplied to the burner 30 is burned within the combined electric power generating equipment 24. The combustion gas rotates the gas turbine 31 and generates electric power while expanding within the gas turbine 31. After burning in the burner 30 of the gas turbine 31 and generating electric power by the gas turbine 31a portion the coal gas 55 is discharged as an exhaust gas 32 from the gas turbine 31. A portion of the exhaust gas 32 becomes a heat source for generating a steam 34 by an exhaust heat recovery boiler 33. Further, the remaining exhaust gas 32 is supplied to the desulfurization apparatus 51 as the sulfur discharge gas 56. After the heat is recovered by the exhaust heat recovery boiler 33, the exhaust gas 32 is discharged to an outer portion. The steam 34, heat-exchanged and produced in the exhaust heat recovery boiler 33, is fed to the steam turbine 35 to generate electric power. A portion of the steam 34 discharged from the steam turbine 35 is condensed in the condenser 36. Then, the condensed steam 34 is again supplied to the exhaust heat recovery boiler 33. The remaining steam 34 is supplied to the gas cooler 28. The steam 34 produced by the heat recovered from the coal gas 11 in the gas cooler 28 is fed to the steam turbine 35. In the sulfur discharge gas 56 containing H2S condensed in the above manner, sulfur is removed in a Claus reactor or in sulfur recovery equipment 63 using a lime plaster process. The gas 56 in which the sulfur is removed is discharged into ambient air as a clean gas 68 (a tail gas). The removed sulfur is recovered. The gas 68 can be reused as a gas passing through the sulfur discharge gas communication passage 53. In the desulfurization apparatus and the electric power plant using the same, the chemical reaction shown in formula (4) occurs in the end of the passage 52 for the gas to be processed in the sulfur moving body 54. Further, the chemical reaction shown in formula (5) occurs in the end of the sulfur discharge gas passage 53 in the sulfur moving body 54. Accordingly, hydrogen sulfide continuously moves to the sulfur discharge gas 56 from the coal gas 55 flowing through the passage 52, so that a concentration of a hydrogen sulfide contained in the sulfur discharge gas becomes higher than the concentration of a hydrogen sulfide contained in the coal gas 55. Therefore, hydrogen sulfide can be efficiently concentrated. Further, the sulfur discharge gas 56 uses the burned exhaust gas 32 flowing out from the gas turbine 31, so that the partial pressure of H2O and CO2 becomes higher than the partial pressure of H2O and CO2 in the coal gas 55. Accordingly, the chemical reaction shown in the formula (5) occurs at the end of the sulfur discharge gas passage 53, so that the reaction largely proceeds to the left direction. Therefor, the concentration of hydrogen sulfide contained in the sulfur discharge gas 56 becomes higher than the concentration of a hydrogen sulfide contained in the coal gas 55, so that hydrogen sulfide can be efficiently condensed. Further, when the difference between the temperature of the sulfur discharge gas 56 and the temperature of the coal gas 55 is large, the chemical reaction is promoted and the recovery rate of the sulfur is improved. Preferably, when the temperature of the sulfur discharge gas 56 is lower than the temperature of the coal gas 55, the chemical reaction is promoted, so that the recovery efficiency of the sulfur is improved. Still further, since the sulfur moving body 54 is constituted of a porous member containing a molten carbonate, the carbonate is in a liquid state at operating temperature, so that the moving speed of an ion becomes higher than if the carbonate was in a solid state, thereby improving the reaction efficiency. Furthermore, since the flow direction of the coal gas 55 and the flow direction of the sulfur discharge gas 56 are different from each other, that is, they flow in direction opposite to each other, the concentration of hydrogen sulfide contained in the sulfur discharge gas 56 increases as it flows, so that the sulfur discharge gas 56 containing a high concentration of hydrogen sulfide can b e finally obtained. . In the embodiment shown in Fig.3, directly opposing flows are illustrated. While directly opposing flows may b e preferred, the embodiment is not limited to directly opposing flows. For example, the flows may cross or may be set at some other angle relative to each other. Next, the structure and operation of a further embodiment not within the scope of the invention will be described below with reference to Fig. 5. In each of the following embodiments, the same reference numerals are attached to the same elements as those of the first embodiment and overlapping explanations will be omitted. The feature of the second embodiment is that the desulfurization apparatus 51 is structured by laminating the sulfur moving bodies 54 and alternately inserting the passage 52 and the sulfur discharge gas passage 53 therebetween. Accordingly, a lot of sulfide can be efficiently recovered from the coal gas 55. Fig. 5 is a cross sectional view of the embodiment of the desulfurization apparatus. The passage 52 and the sulfur discharge gas passage 53 are alternately layered along with planar sulfur moving bodies 54, thereby constituting the desulfurization apparatus 51. The flow directions of the coal gas 55 and the sulfur discharge gas 56 are different from each other. That is, they flow in directions opposite to each other. In this embodiment of the desulfurization apparatus mentioned above, by increasing the reaction area for producing a sulfide ion from the sulfide supplied to the sulfur moving body 54, the desulfurization process is performed to a large amount of coal gas 55, so that the sulfide can be recovered. Further, the desulfurization apparatus 51 can be made compact by layering the sulfur moving bodies 54. Next, the structure and operation of an embodiment in accordance with the invention will be described below with reference to Figs. 6(a) and 6(b). The feature of this embodiment is that the desulfurization apparatus 51 is structured by disposing the sulfur moving bodies 54 in a honeycomb manner. A lot of sulfide can be efficiently recovered from the coal gas 55. Fig. 6(a) is a front elevational view of the embodiment of the desulfurization apparatus in accordance with the invention and Fig. 6(b) is a cross sectional view along a line A-A in Fig. 6(a). The cylindrical sulfur moving bodies 5 4 are disposed in a honeycomb manner. A partition plate 64 having an opening portion 61 is provided in one end in a longitudinal direction of the sulfur moving body 54. The other end of the sulfur moving body 54 is closed. A supply manifold 62 for supplying the coal gas 55tothesulfur moving body 54 from the opening portion 61 and a recovery manifold 63 for recovering the sulfur discharge gas 56 from the opening portion 61, are provided in the opening portion 61 end of the sulfur moving body 54. The sulfur discharge gas 56 is discharged from four opening portions 61 adjacent to one opening portion 61 from which the coal gas 55 is supplied. The coal gas 55 supplied from the supply manifold 62 reaches the cylindrical sulfur moving body 54 from the opening portion 61. The sulfide ion is produced in the sulfur moving body 54. The sulfide is produced by the produced sulfide ion. The produced sulfide is exhausted from the exhaust manifold 63 through the opening portion 61 by the sulfur discharge gas 56. In this embodiment of the desulfurization apparatus mentioned above, by increasing the reaction area for producing a sulfide ion from the sulfide supplied to the sulfur moving body 54, the desulfurization process is performed to a large amount of coal gas 55. Accordingly, the sulfide can be efficiently recovered. Further, the desulfurization apparatus 51 can be made compact by layering the sulfur moving bodies 54. Next, a structure and an operation of a further embodiment not within the scope of the invention will be described below with reference to Fig. 7. According to this embodiment, the desulfurization apparatus 51 is structured by disposing the sulfur moving bodies 54 in a shell tube manner. A lot of sulfide can be efficiently recovered from the coal gas 55. Fig. 7 is a schematic view of the embodiment of the desulfurization apparatus. A plurality of cylindrical sulfur moving bodies 54 are disposed. A hollow portion of the sulfur moving body 54 becomes a supply manifold 62 for supplying the coal gas 55 to the sulfur moving body 54. Further, a hollow cylindrical recovery manifold 63 for housing a plurality of sulfur moving bodies 54 therewithin is provided. The recovery manifold 63 recovers the sulfur discharge gas 56 discharged from the sulfur moving body 54. A plurality of sulfur moving bodies 54, a plurality of supply manifolds 62, and the recovery manifold 63 are disposed in a shell tube manner. The coal gas 55 supplied from the supply manifold 62 reaches the cylindrical sulfur moving body 54. The sulfide ion is produced in the sulfur moving body 54. The sulfide is produced by the produced sulfide ion. The sulfide thus produced is discharged from the exhaust manifold 63 through the sulfur discharge gas 56. In this case, the flow direction within the supply manifold 62 and the flow direction within the recovery manifold 63 are opposed to each other. Further, when a diameter of the supply manifold 62 is made small, the concentration of the sulfide contained in the coal gas55can be made small. Further, in the case of using the desulfurization apparatus 51 having the above structure for an electric power plant, since the pressure within the supply manifold 62 is higher than the pressure within the recovery manifold 63, it is suitable to dispose the recovery manifold 63 within the sulfur moving body 54 and dispose the supply manifold 62 in the outer side of the sulfur moving body 54. By making the structure in the above manner, even when a thickness of the sulfur moving body 54 is thin and a curvature thereof is large, the structure can sufficiently withstand the pressure from the outer portion. In this embodiment of the desulfurization apparatus by increasing the reaction area for producing a sulfide ion from the sulfide supplied to the sulfur moving body 54, the desulfurization process can be performed for a large amount of coal gas 55. Further, since the diameter of the supply manifold 62 is made small, the concentration becomes small, so that desulfurization can be efficiently performed. Still further, the desulfurization apparatus 51 can be made compact by disposing a plurality of the sulfur moving bodies 54 in a shell tube manner. Furthermore, the manufacture thereof can be easily performed. Moreover, the manufacturing cost for the desulfurization apparatus 51 can be reduced. In this case, it is needless to say that the invention is not limited to the embodiment mentioned above, and can be variously modified and realized in a range within the scope of the invention as defined by the appended claims. For example, it is not necessary to directly use the exhaust gas from the gas turbine for the sulfur discharge gas, and it is possible to use the gas from which the sulfur is removed in the sulfur recovery equipment for the sulfur discharge gas where the desulfurization apparatus and the sulfur recovery equipment are a closed loop.

Claims: Desulfurization apparatus, comprising: a plurality of sulfur moving bodies (54) capable of diffusing sulfide ion from sulfur containing gas (55) which form gas passages accessible via opening portions (61) and have a planar plate shape; at least one supply manifold (62) for supplying the sulfur containing gas (55) to the sulfur moving bodies (54), the at least one supply manifold (62) being in communication with a plurality of the opening portions (61); at least one recovery manifold (63) for recovering sulfur discharge gas in communication with a plurality of other of the opening portions (61), wherein the at least one supply manifold (62) and the at least one recovery manifold (63) are arranged in an alternating manner; characterized in that the plurality of sulfur moving bodies (54) include a molten carbonate impregnated into a porous member to which a ceramic is sintered and are disposed in two directions in a honeycomb array; and the at least one supply manifold (62) and the at least one recovery manifold (63) extend at a diagonal to the directions of the arrays of the sulfur moving bodies (54). Desulfurization apparatus as claimed in claim 1, characterized in that , the two directions are transfers directions.

Inventors: HORI MICHIO, MURATA KEIJI, OGAWA TAKASHI, YAMASHITA KEIJIRO, HORI, MICHIO, MURATA, KEIJI, OGAWA, TAKASHI, YAMASHITA, KEIJIRO
Applicants: TOSHIBA KK, KABUSHIKI KAISHA TOSHIBA
Application year: 1998
Main classification: B01D53
IPC codes: B01D53, C01B17, C10K1