The present invention, waste in a system for generating electric power in a gas turbine or gas engine using a flammable gas obtained by reforming gasification-reforming, with a high removal rate of the acid component removal of the hot gasification gas on the achievement apparatus used to implement the method and method for.
BACKGROUND
[0002]
　Recently, to deal with global warming correspondence strongly demanded, in power generation using waste power generation efficiency and with steam temperature high temperature waste incineration power generation (BTG generation), waste gasified-modified system for power generation in gas turbines and gas engines using the combustible gas has been studied.
[0003]
　In such a power generation system, incombustible and various metals, especially gasification of wastes containing metallic aluminum is generally 700 ° C. or less, usually carried out at about 500 ~ 650 ° C.. Gasified gas, char and tar component of unburned reformed into combustible gas by steam in the reforming furnace. Reforming reaction, at about 1000 ~ 1200 ° C. in the case of performing in the absence of a catalyst, when using a catalyst is performed at about 800 ~ 1000 ° C..
[0004]
　For example, Patent Document 1, gasification furnace, the high temperature dust collector equipment, tar decomposition facilities, gasification power generation system consisting of purified facilities are described. In this gasification power generation system, 800 ~ 900 ° C. of gas produced in the gasification furnace after being dust at a high temperature dust collector installation comprising a ceramic filter or the like, the tar decomposition facility having a cracking catalyst, such as tar It is delivered.
[0005]
　During waste gasified gas, in addition to unburned char and tar H 2 and CH 4 combustible gas such as, CO, CO 2 derived and dust, halogen or S contained in waste HCl and SO 2 , SO 3 gas and the like.
[0006]
　When performing the reforming reaction using a catalyst, although the reforming catalyst of the nickel-based or noble metal is used, HCl and SO contained in the gas gasified 2 , SO 3 is the reforming catalyst by a gas such as the It is poison. Such, in order to prevent the poisoning of the reforming catalyst, it is necessary to remove the gas components poisoning upstream of the reformer. However, in a high temperature dust collector installation according to Patent Document 1 because it is not carried out desalting and desulfurization simply performs dust removal, the performance of the catalyst for decomposing tar content may decrease.
[0007]
　Conventionally, as desalination and desulfurization technology of waste incineration system or the like according to the dry method, slaked lime in the exhaust gas (Ca (OH) 2 ) and sodium bicarbonate (NaHCO 3 ) or the like blowing the powder medicament, solid reaction product object technology to be removed by bag filter has been known. This technique is applied to the exhaust gas temperature range of 0.99 ~ 200 ° C., the temperature is lower the removal efficiency. A technique for purifying pyrolysis gas by applying such a technique is disclosed (Patent Document 2). One technique disclosed in Patent Document 2, the purification of the pyrolysis gas, and a bag filter for dust removal, is performed by the second bag filter for desalination. Dust-removed pyrolysis gas before with slaked lime or calcium oxide in the second bag filter (CaO), calcium carbonate, sodium bicarbonate, sodium carbonate (Na 2 CO 3 is mixed with an alkaline agent such as), However, in this temperature range will be HCl to compete with carbon dioxide, in order to obtain a high HCl removal rate requires many drugs. Moreover, since the bag filter of the dust removal is not performed desalting and desulfurization, there is a possibility that the thermal decomposition gas purification may be insufficient.
[0008]
　Further, after drying the mixture of sodium carbonate and alumina sol, sodium aluminate (NaA1O be produced by grinding and calcining 2 ) based halide absorber is disclosed (Patent Document 3). The particle size of the halide-absorbing agent is at 250 ~ 500 [mu] m, and evaluated halide removal performance at 400 ° C. using a fixed bed flow system in Patent Document 3 reactor. However, in a temperature range of below 500 ° C., is performed dry desalted and desulfurization established a fixed bed flow reactor in the pyrolysis gas flue waste, which are tar adheres to dust and char fixed secured to halogenating absorbent bed flow reactor, it can not be stable operation by an increase in pressure loss due to clogging. For example, in a filtration test using polystyrene as the oil component (tar ingredients), the polystyrene is attached to the filter, polystyrene attached to the filter is removed the oil is heated at a temperature of above 500 ° C. based on the pressure loss Back it has been reported (non-Patent Document 1).
CITATION
Patent Document
[0009]
Patent Document 1: JP 2006-037012 Patent Publication
Patent Document 2: JP 2002-130628 Patent Publication
Patent Document 3: Japanese Patent No. 3571219
Non-patent literature
[0010]
Non-Patent Document 1: Shoichi Ogawa, other, collecting and reproducing characteristics of the hydrocarbon components of polystyrene pyrolysis gas by the ceramic filter, the Society of Powder Technology, Vo1.40No. 11, p19-25,2003
Summary of the Invention
Problems that the Invention is to Solve
[0011]
　The present invention is to solve the problems of the prior art described above, it is possible to achieve a high desalination and desulfurization performance in the high temperature range, and the pressure loss due to clogging of the device by adhering tar dust and char It does not cause a rise in, and to provide an acid component removing method and apparatus for a high temperature in the gasification power generation system.
Means for Solving the Problems
[0012]
　The present invention was made in order to achieve the above object, including the following aspects.
[0013]
　(1) and the gasification step of partial combustion gasification of the gasification material, a cyclone treatment step of coarse powder trapping processing gasification gas from the gasification step, coarse powder-removed exiting the cyclone processing step a bag filter processing step of dust removal processing gasification gas, the bag filter exits the process dedusting been gasified gas CO 2 CO handle absorbs reforming 2 and absorbed-reforming step, the CO 2 absorption and modification in the gasification power generation system including a power generation process using the reformed gas exiting the process for generating power,
　in front of and the cyclone process after the gasification step, the cyclone upstream added with desalted and desulfurization function agent, using said gas exiting from the generator step as an additive a carrier gas after heat recovery, to supply to the gasification gas, and
　the CO 2 CO used in the absorption-modifying step 2 intake Agent gas temperature range 450 ~ 700 ° C., preferably CO in a temperature range of 540 ~ 640 ° C. 2 is absorbed, CO 2 when the absorption amount reaches saturation, the flow of oxygen or air for the reforming catalyst SoNoboru temperature CO 2 switched to immediately upstream of the absorbent filler layer, the same absorbent filler layer 800 ~ 950 ° C., preferably CO 2 from the absorbent by heating to a temperature range of 850 ~ 900 ° C. 2 and characterized in that disengaging the to,
Acid component removing method at high temperatures in the gasification power generation process.
[0014]
　(2) the cyclone upstream additive CO 2 also has an absorption and removal capabilities, the acid component removing method at high temperatures in the gasification power generation method according to (1).
[0015]
　(3) the average particle diameter of the cyclone upstream additive characterized in that it is a 100 ~ 1000 .mu.m, wherein (1) or an acid component removing method at high temperatures in the gasification power generation method according to (2).
[0016]
　(4) the cyclone upstream additives, fired dolomite, slaked lime, characterized in that it is selected from the group consisting of sodium aluminate and sodium bicarbonate, the (1) gasification of any one of the - (3) acid component removing method at a high temperature in the power generation process.
[0017]
　(5) the cyclone treatment before after and the bag filter process steps, desalted and has a desulfurizing capability and the cyclone upstream additives and identical even with good cyclone downstream additives be different also a is, burnt dolomite, hydrated lime, an additive selected from the group consisting of sodium aluminate and sodium bicarbonate, the gas exiting from the generator step using as an additive a carrier gas after heat recovery, coarse powder-removed gasification gas and supplying to, (1) to (4) acid component removing method at high temperatures in the gasification power generation method according to any one of the.
[0018]
　(6) collecting the coarse powder containing the additives in the cyclone processing step, and supplying to the gasifying step and the collecting crude powder with the gasification material, (1) acid component removing method at high temperatures in the gasification power generation process according to any one of the - (5).
[0019]
　(7) The CO 2 CO used in the absorption-modifying step 2 absorbent CaO, Ca (OH) 2 , wherein the selected from the group consisting of and burnt dolomite, either (1) to (6) acid component removing method at high temperatures in the gasification power generation method according to 1.
[0020]
　(8) CO by aqueous NaOH said reformed gas after the heat recovery process 2 to absorption treatment, Na occurred 2 CO 3 , and recovering and removing, in any one of (1) to (7) acid component removing method at high temperatures in the gasification power generation method according.
[0021]
　(9) and the gasification furnace for partial combustion gasification gasification material, the gasification gas from the furnace is installed downstream of the gasification furnace and the cyclone for coarse powder collecting process, downstream of the cyclone a bag filter installed to dust removal processing exiting crude powder-removed gasification gas from here, the installed downstream of the bag filter dust removal has been gasified gas exiting from this CO 2 treating absorbing reforming CO 2 absorption-reformer, the CO 2 in the gasification power generation system including a power generation facility that generates electricity by utilizing a reformed gas exiting installed in the furnace downstream of the absorption-reformer,
　the gasification furnace the flow path to the cyclone from the cyclone upstream additive supply line for supplying an additive having a desalting and desulfurization function is provided, a carrier gas line coming from the power generation equipment in the supply line is connected, the CO 2 absorption and reformer of CO 2 CO immediately upstream of the absorbent filler layer 2 absorption amount of oxygen or air for reforming RoNoboru temperature when reached saturation CO 2 switches to the absorbent filler layer oxygen or air supply wherein the line is connected,
the acid component removing device at a high temperature in the gasification power generation system.
[0022]
　(10) the flow path from the cyclone to the bag filter, cyclone downstream additive supply line for supplying an additive having a desalting and desulfurization function is provided, a carrier gas line coming from the power plant to the feed line wherein the but are connected,
the acid component removing device at a high temperature in the gasification power generation system according to (9).
[0023]
　The average particle diameter of the particles is a value measured by a laser diffraction particle size distribution measuring apparatus.
[0024]
　Throughout this specification and claims, the resulting gas by partial combustion gasification of the gasification material that [gasification gas.
Effect of the invention
[0025]
　According to the present invention, before the cyclone process, by supplying the gasification gas to the cyclone upstream additives with desalting and desulfurization function, yet in front of the bag filter processing step, desalting and desulfurization function a cyclone downstream additive by supplying the gasification gas with respect to the high temperature region of the gasification gas such as 450 ~ 700 ° C., it is possible to achieve a high desalination and desulfurization performance, the reforming catalyst it is possible to prevent the poison.
[0026]
　Further, it is possible to prevent the problem of causing an increase in pressure loss due to clogging of the device by adhering tar dust and char by using additives such as described above.
[0027]
　Furthermore, CO 2 CO used in the absorption-modifying step 2 absorbent CO gas temperature range 450 ~ 700 ° C. 2 is absorbed, CO 2 when the absorption amount reaches saturation, oxygen or for the reforming catalyst SoNoboru temperature the flow of air CO 2 switch to immediately upstream of the absorbent filler layer, CO from the absorbent by heating the same absorbent filler layer to a temperature range of 800 ~ 900 ° C. 2 by disengaging the, gasification gas of CO 2 can be removed efficiently and permanently.
BRIEF DESCRIPTION OF THE DRAWINGS
[0028]
[1] Figure 1 is a flow diagram of a gasification power generation system according to the embodiment of the present invention.
FIG. 2 is a graph and table showing the relationship between the desalination and desulfurization agent and desalted and desulfurization performance.
[Figure 3-1] Figure 3-1 is a graph showing the relationship between various desalting and desulfurizing agent and desalted and desulfurization performance (temperature: 550 ° C.).
[Figure 3-2] Figure 3-2 is a graph showing the relationship between various desalting and desulfurizing agent and desalted and desulfurization performance (temperature: 600 ° C.).
[Figure 3-3] Figure 3-3 is a graph showing the relationship between various desalting and desulfurizing agent and desalted and desulfurization performance (temperature: 650 ° C.).
DESCRIPTION OF THE INVENTION
[0029]
　Examples of the present invention with reference to the accompanying drawings. However, this is not intended to limit the scope of the present invention.
[0030]
　First, the description according to Figure 1 for the gasification power generation system.
[0031]
　Gasification power generation system includes a gasification furnace 1 for partial combustion gasification of the gasification material, the bag filter 3 to the gasification gas to dust exiting the furnace is installed downstream of the gasification furnace 1, the bag filter 3 CO reforming process dust removal pre gas is installed downstream 2 and the absorption-reformer 4, CO 2 is installed downstream of the absorption-reformer 4 by using the reformed gas leaving the same furnace power and a power generation facility 5 to perform.
[0032]
　The flow path from the gasification furnace 1 to the bag filter 3, a cyclone 2 is placed on the upstream side passage of the cyclone 2, preferably has a desalination and desulfurization function further de-CO 2 additive also functions cyclone upstream additive feed line 6 is connected to supply the additive container 8. Further, the flow path from the cyclone 2 to the bag filter 3, preferably has a desalination and desulfurization function further de-CO 2 cyclone downstream additive supply line 7 for supplying the additive also has a function from the additive container 10 It is provided.
[0033]
　Each starting end of the cyclone upstream additive feed line 6 and the cyclone downstream additive supply line 7, low temperature boiler 13 from the power generation facility 5, a carrier gas line 9 through the dehumidifier 14, booster 15 and the tank 16 It is connected.
[0034]
　The CO 2 CO absorption-reformer 4 2 immediately upstream of the absorbent filler layer, CO 2 CO flow of oxygen or air for reforming RoNoboru temperature when the absorbed amount reaches the saturated 2 absorbent filler layer oxygen or air supply line 19 is switched to is connected. The line 19 is normally CO 2 for supplying oxygen or air for heating immediately upstream of the catalyst-packed layer of the absorbent-reformer 4.
[0035]
　Then, according to the present invention in accordance with the flow diagram of FIG. 1 will be specifically described for each step of the acid component removing method at high temperatures in the gasification power generation process.
Gasification process
　waste, RDF, to partial combustion gasification in the gasification furnace 1 the gasification materials such as wood chips. The gasification furnace 1 oxygen and water vapor is supplied from the furnace bottom.
[0036]
Cyclone process
　gas gases leaving the furnace top gas furnace 1 is sent to a cyclone 2, the particles in the gasification gas is divided into an average particle diameter of 100μm or more coarse powder and the average particle size 100μm less fine powder . The temperature of the gas entering the cyclone 2 is 700 ° C. or less, preferably 550 ~ 650 ° C., the temperature of the gas leaving the cyclone 2 is 550 ~ 650 ° C..
[0037]
　Additives having a desalting and desulfurization function from the cyclone upstream additive feed line 6 to the upstream side passage of the cyclone 2 is blown. The additive is preferably CO in addition to desalting and desulfurization function 2 also has an absorption and removal function. This is a one which can be converted to the chloride or sulfate at 700 ° C. or less, are preferably selected from the group consisting of calcined dolomite, hydrated lime, sodium aluminate and sodium bicarbonate. The average particle diameter of the additive is preferably 100 ~ 1000 .mu.m, more preferably 300 ~ 600 .mu.m. Preferably burnt dolomite in cost, sodium aluminate are preferable in terms of desalination and desulfurization rate. In this example, it was fed to a cyclone upstream by the line 6 a burnt dolomite with an average particle size of a few hundred μm from the additive container 8.
[0038]
　Has a desalting and desulfurization function on the upstream side passage of the cyclone 2, preferably CO 2 by blowing additive having also absorption-removing function, desalted and desulfurization treatment gasification gas, preferably decarboxylation it is possible to process, self-cleaning action of dust and tar adhering to the cyclone 2 can be performed, reducing the pressure loss in the downstream of the bag filter, it is possible to perform the operation without hindrance. Some or all of the crude powder additive having an average particle diameter of 100 ~ 1000 .mu.m by the cyclone, dust, tar was recovered at the bottom and supplied to the gasification furnace 1 the collected substance with the gasification material. Thus it is possible to complement the modification of the tar in the downstream of the CO 2 absorption-reformer 4.
[0039]
Bag filter process
　crude powder-removed gasification gas exiting followed cyclone 6 is fed to a bag filter 3 for dust removal treatment of the same gas. Crude powder-removed gasification gas containing particles having an average particle size of less than 100 [mu] m.
[0040]
　The flow path from the cyclone 2 to the bag filter 3, the cyclone downstream additive supply line 7, the additive having a desalting and desulfurization function is blown. The additive is preferably CO in addition to the de-desalination and desulfurization function 2 also has an absorption and removal function. The additive, there is capable of being converted to the chloride or sulfate at 700 ° C. or less, it is preferably selected from the group consisting of calcined dolomite, hydrated lime, sodium aluminate and sodium bicarbonate. The average particle size of the additive is preferably 20μm or less, more preferably 15μm or less. Preferably burnt dolomite in cost, sodium aluminate are preferable in terms of desalination and desulfurization rate. Cyclone downstream additive may be heterologous in the cyclone upstream additives and the like. In this example, it was fed to a cyclone downstream side by the cyclone downstream additive supply line 7 the burnt dolomite with an average particle size of 20μm or less from the additive tank 10.
[0041]
　Has a desalting and desulfurization function on the downstream side passage of the cyclone 2, preferably CO 2 by blowing additive having also absorption-removing function, desalted and desulfurization processes coarse powder-removed gasification gas preferably it is decarbonated. In particular by desalting and desulfurization process, downstream of the CO 2 can extend the life of the Ni-based reforming catalyst is generally used in the absorption-reformer 4.
[0042]
　The average particle diameter of the additives, desalination, in order to enhance the effect of desulfurization, and preferably 20μm or less. It may be used in combination of known filter aid cyclone downstream additives.
[0043]
　The average particle diameter of the particles is a value measured by a laser diffraction particle size distribution measuring apparatus.
[0044]
　In this example, a bug filter 3, to prevent adhesion to the filter cloth dust containing tar, used precoat bag filter in order to improve the peelability of the cake layer of filter cloth surface. The temperature of the gas entering the pre-coat bag filter is 550 ~ 650 ° C., the temperature of the gas exiting the same bag filter is lowered to about 540 ~ 640 ° C. due to heat dissipation. When the pressure loss is increased in the pre-coat bag filter, the cake layer of the filter cloth surface flicked by a pulse-jet system, then the cyclone downstream additives, or those which in combination with a filter aid in the additive short in, to pre-coat the filter cloth surface. Pressure loss during precoat and aim the 0.5 ~ 0.6 kPa. Brushing the cake layer of the filter cloth surface, the pressure loss is preferably from ~ 1.8 kPa 1.5 (153.0 ~ 183.5MmH 2 performed when the range of O).
[0045]
　The amount of precoat, HCl + SO in the gas 2 is blown 3 equivalents at about 20 minutes. It is a measure that is about 3.5 hours as one cycle as the sum of the time required for the precoat and steady operation time. Brushing by the pulse jet is preferably carried out by the pressure loss control bugs.
[0046]
CO 2 absorption and modifying step
　gasification gas, after being dust in the bag filter 3, CO 2 is fed to the absorber-reformer 4. CO 2 is the top of the absorption-reforming furnace 4 CO 2 is filled absorbent, reforming catalyst is filled in the lower part. CO 2 as the absorbent, 450 ~ 700 ℃, preferably CO in a temperature range of 540 ~ 640 ° C. 2 carbonation proceeds by absorption, 800 ~ 950 ℃, preferably decarboxylation i.e. CO in a temperature range of 850 ~ 900 ° C. 2 compound desorption occurs is used. CO 2 Examples of absorbents, CaO, Ca (OH) 2 , calcined dolomite (CaO · MgO) and the like, CO in this example 2 using CaO as an absorbent.
[0047]
　CO by switching the oxygen or the flow path of the air supply line 19 2 CO from the absorbent 2 is explained desorption.
1) normal CO 2 during the absorption operation temperature range of the gasification gas is 450 ~ 700 ° C., preferably 540 ~ 640 ° C., CO 2 temperature of the absorption agent is also held in this temperature range. CO 2 When using a CaO as an
　　absorbent, CaO + CO 2　→ CaCO 3　
CO according to reaction of 2 is absorbed and removed by the absorbent. Thus CO in the gasification gas 2 shift reaction follows by removing proceeds readily to the right.
[0048]
　　+ H CO 2 O → CO 2 + H 2
　oxygen or air heating in this state is supplied to the immediately upstream of the reforming catalyst layer by oxygen or normal flow path of the air supply line 19.
2) CO 2 when the absorption amount reaches saturation, during normal operation the oxygen or air which has been used to increase the temperature of the catalyst-packed layer, by switching the flow path of the oxygen or air supply line 19, CO 2 absorbent filler layer supplied to the immediately upstream, of the same absorbent 800 ~ 950 ° C., preferably heated to a temperature range of 850 ~ 900 ° C.. This temperature range is CO 2 carbonate of absorbent CO pyrolyzed 2 is desorbed from the absorbent.
[0049]
　CO 2 heated by the injection of oxygen or air in the absorption-reformer 4, tar components and H 2 , CO, CH 4 produced by the oxidation reaction heat of.
[0050]
　CO 2 CO absorbent 2 the absorption reaches saturation, CO gasification gas provided downstream of the high-temperature boiler 11 2 downstream CO represents the concentration 2 since the value of the analyzer 18 begins to rise, above oxygen or air heating CO as 2 supplied to immediately upstream of the absorbent filler layer. The absorber 800 ~ 950 ° C., preferably when heated to a temperature range of 850 ~ 900 ° C., CaCO 3 is started to decompose, resulting CO 2 flows to the downstream side. This time CO in the gasification gas 2 so temporarily increasing the concentration of the shift reaction is not promoted. CO 2 is provided upstream of the absorption-reformer 4 CO in the gasification gas 2 upstream CO represents the concentration 2 and analyzer 17 the downstream CO 2 CO respectively represented by the spectrometer 18 2 approaching concentration Then, to return the flow of oxygen or air for heating to the immediate upstream of the reforming catalyst layer, the temperature of the catalyst-packed layer 450 ~ 700 ° C., preferably down to a range of 540 ~ 640 ° C..
[0051]
　After that operation of the above 1) and 2) are repeated.
[0052]
　CO 2 CO by absorbent filler layer 2 by removing the can promote the following shift reaction in the reforming catalyst packed layer.
[0053]
　Assuming toluene as a representative example of tar, CO 2 main reactions occurring in the absorption-reformer 4 is as follows.
[0054]
　i) C 7 H 8 +. 9O 2　→ 7Co 2 + 4H 2 O · · oxidation reaction
　ii) C 7 H 8 + 7H 2 O → 7Co + 11H 2　· reforming reaction
　iii) CO + H 2 O → CO 2 + H　2 · · · · shift reaction
　iv) Others, when oxygen is present in excess, H 2 , CO, CH 4 also occurs oxidation reaction or the like.
[0055]
Cooling tower process
　CO 2 850 ~ 900 ° C. of the hot gases leaving the bottom of the absorption-reformer 4, wherein sent to the high-temperature boiler 11 after the heat recovery process, the cooling tower 12 at a temperature 170 ~ 180 ° C. Sent. The cooling tower 12 are circulating aqueous NaOH which CO in gasification gas by 2 is absorbed, resulting Na 2 CO 3 salt is recovered and removed. Therefore, greenhouse gases are not discharged.
[0056]
Power step
　cooling tower 12 Temperature 55 ~ 60 ° C. of cold gas leaving the is sent to the power generation facility 5 with a gas turbine or gas engine, is used here for power generation.
[0057]
Carrier gas
　after the temperature 400 ° C. of the gas discharged from power generation equipment 5 then that is heat recovery processed by cold boiler 13, a portion is released into the atmosphere at 170 ~ 180 ° C., the remainder being dehumidified by the carrier gas line 9 14 , booster 15 and through the tank 16 is sent to the starting end of the cyclone upstream additive feed line 6 and the cyclone downstream additive supply line 7, the carrier gas of the cyclone upstream additives and cyclone downstream additive ( is used as the gas temperature 50 ° C.). The oxygen concentration of the gas is about 1-2% by volume, since the injection rate of the carrier gas to the outlet gas of the gasification furnace is 1/15 to 1/30, the lower heating value by combustion of the combustible gas It does not cause a reduction in the (LHV).
[0058]
Experimental Example
　The following experiments of the present invention.
[0059]
　Waste for generating electric power by utilizing the combustible gas obtained by reforming gasification-reforming, in the system shown in FIG. 1, an experiment was conducted by changing each condition. An example of the composition of the outlet gas of the gasification furnace 1 in Table 1, the gasification furnace 1 and CO 2 air ratio in Table 2 with respect to the temperature and the outlet gas of the absorption-reformer 4, and desalting and desulfurizing agent the relationship between the desalination and desulfurization performance in Figure 2, the air ratio to the outlet gas of the power generation facility 5 in Table 3, the relationship between the desalination and desulfurization performance and various locations desalting and desulfurizing agent in Table 4 and Figure 3, calcium carbonate generation and degradation (CaO + CO of 2 ⇔CaCO 3 results of the thermodynamic equilibrium calculations for) Table 5, respectively.
[0060]
　According to Table 5, CO 2 in the absorption tower, the inlet CO 2 in the 8.1%, 600 ° C. At equilibrium calculations on 96.98% of CO 2 in is to be absorbed and removed (650 ° C. 89.37 %). Further, when raising the temperature of the absorption tower 850 ° C., an outlet CO 2 (decomposed until 900 ° C. in 79.48%) it to become the concentration is decomposed until 38.59%.

WE claims

[Requested item 1]
　A gasification step of partial combustion gasification of the gasification material, a cyclone treatment step of coarse powder trapping processing gasification gas from the gasification step, coarse powder-removed gasification gas from the cyclone processing step a bag filter processing step of dust removal processing, dust removal has been gasified gas CO exiting the bag filter step 2 CO treating absorb reforming 2 and absorbed-reforming step, the CO 2 leaving the absorption-reforming process in the gasification power generation system including a power generation process for generating electric power by utilizing the reformed gas,
　in front of and the cyclone process after the gasification step, the cyclone upstream additives with desalting and desulfurization function, using said gas exiting from the generator step as an additive a carrier gas after heat recovery, to supply to the gasification gas, and
　the CO 2 CO used in the absorption-modifying step 2 absorbent Scan temperature range 450 ~ CO in a temperature range of 700 ° C. 2 is absorbed, CO 2 when the absorption amount reaches saturation, the flow of oxygen or air for the reforming catalyst SoNoboru temperature CO 2 immediately upstream of the absorbent filler layer to switch, CO from the absorbent by heating the same absorbent filler layer to a temperature range of 800 ~ 950 ° C. 2 , characterized in that disengaging the,
acid component removal process at high temperatures in the gasification power generation process.
[Requested item 2]
　The cyclone upstream additive CO 2 also has an absorption and removal capabilities, the acid component removing method at high temperatures in the gasification power generation method according to claim 1.
[Requested item 3]
　The average particle diameter of the cyclone upstream additive characterized in that it is a 100 ~ 1000 .mu.m, acid component removal process at high temperatures in the gasification power generation method according to claim 1 or 2.
[Requested item 4]
　The cyclone upstream additives, fired dolomite, slaked lime, characterized in that it is selected from the group consisting of sodium aluminate and sodium bicarbonate, at elevated temperature in the gasification power generation process according to any one of claims 1 to 3 acid component removing methods.
[Requested item 5]
　Wherein after cyclone treatment step and before the bag filter processing step, a a and the cyclone upstream additives and good cyclone downstream additives be different even in the same desalting and desulfurization function supplies burnt dolomite, hydrated lime, an additive selected from the group consisting of sodium aluminate and sodium bicarbonate, the use of a gas exiting from the generator step as an additive a carrier gas after heat recovery, the coarse powder-removed gasification gas wherein the acid component removing method at high temperatures in the gasification power generation method according to any one of claims 1-4.
[Requested item 6]
　And collecting the coarse powder containing the additives in the cyclone processing step, and supplying to the gasifying step and the collecting crude powder with the gasification material of claims 1 to 5, acid component removing method at high temperatures in the gasification power generation method according to any one.
[Requested item 7]
　The CO 2 absorption and modification used in step CO 2 absorbent CaO, Ca (OH) 2 , wherein the selected from the group consisting of and burnt dolomite, as claimed in any one of claims 1 to 6, acid component removing method at high temperatures in the gasification power generation process.
[Requested item 8]
　The reformed gas CO on aqueous NaOH after heat recovery process 2 to absorption treatment, Na occurred 2 CO 3 and recovering and removing characterized gasification according to any one of claims 1 to 7 acid component removing method at a high temperature in the power generation process.
[Requested item 9]
　A gasification furnace for partial combustion gasification of the gasification material, a cyclone for coarse powder trapping processing gasification gas exiting the furnace is installed downstream of the gasification furnace, it is installed downstream of the cyclone a bag filter for dust removal processing exiting crude powder-removed gasification gas from here, the installed downstream of the bag filter dust removal has been gasified gas exiting from this CO 2 treating absorbing reforming CO 2 absorption and Kai and quality furnace, the CO 2 in the gasification power generation system including a power generation facility that generates electricity by utilizing a reformed gas exiting installed in the furnace downstream of the absorption-reformer,
　the cyclone from the gasification furnace the flow path to the cyclone upstream additive supply line for supplying an additive having a desalting and desulfurization function is provided, a carrier gas line coming from the power generation equipment in the supply line is connected, the CO 2 absorption Reforming furnaces CO 2 CO immediately upstream of the absorbent filler layer 2 absorption amount of oxygen or air for reforming RoNoboru temperature when reached saturation CO 2 oxygen switched to absorbent filler layer or the air supply line is characterized in that it is connected,
the acid component removing device at a high temperature in the gasification power generation system.
[Requested item 10]
　The flow path from the cyclone to the bag filter, cyclone downstream additive supply line for supplying an additive having a desalting and desulfurization function is provided, a carrier gas line coming from the power generation equipment in the supply line is connected wherein the are,
the acid component removing device at a high temperature in the gasification power generation system of claim 9.