JP2011255375A - Method for producing gasification catalyst, and gasification treatment system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for producing a gasification catalyst, capable of showing sulfur resistance and coking resistance, and further showing high activity though Ni hardly solid-dissolves, even when operating at a low furnace temperature of 1,000°C or below without using an expensive noble metal-based catalyst.SOLUTION: In this method for producing a gasification catalyst, one kind or two or more kinds of tungsten salts, cobalt salts and molybdenum salts are mixed with nickel sulfate and magnesium oxide, to generate a complex reaction, and a complex is dehydrated, cleaned, mixed with a calcium raw material, then dried and calcined.

Description

  The present invention relates to a method for producing a gasification catalyst and a gasification treatment system, and more particularly, when gasifying and utilizing an organic gasification product, the tar content can be effectively suppressed even if gasification treatment is performed at 1000 ° C. or lower. The present invention relates to a method for producing a gasification catalyst and a gasification treatment system.

  In recent years, techniques for using organic gasification products such as biomass (quantitative biological resources) and sewage sludge as fuel are prosperous, and methods for gasifying and treating them are advancing. In the process of gasifying biomass and sewage sludge, the furnace temperature of the gasifier is usually set to 1000 ° C or higher, but if it is lower than this temperature, part of the fuel is converted into tar and char, and the gas This is because the conversion efficiency is lowered and these tars and chars are accumulated in the furnace, which hinders operation.

  Therefore, in order to keep the inside of the furnace at a high temperature of 1000 ° C. or higher, it is necessary to increase energy consumption by burning a large amount of fuel or increasing the oxygen concentration as a gasifying agent using a PSA (oxygen production apparatus). In addition, in order to maintain the temperature at a high temperature, it is necessary to use an expensive furnace material having excellent heat resistance, which increases the operating cost.

  Therefore, a gasification method has been proposed in which the furnace temperature is about 800 ° C. For example, in the case of a fluidized bed gasifier, the generation of tar is suppressed by using a Ni-based catalyst such as a steam reforming catalyst as the fluid medium, or the catalyst is generated by using a catalyst in the subsequent tar decomposition facility. Attempts have been made to modify the tar content. However, there is a problem that Ni in the catalyst is easily poisoned by sulfur poisoning, or there is a problem of carbon deposition (coking), which is not sufficient in actual operation, especially for polycyclic aromatic tars such as naphthalene. It is not effective for this.

As a catalyst that has been known for a long time, a catalyst based on Al ₂ O ₃ such as Ni / Al ₂ O ₃ or Ni / Al ₂ O ₃ .CaO has a problem of coking. Although the catalyst based on MgO suppresses the occurrence of coking, there is a problem that Ni and MgO as active components are easily dissolved, and the solidified Ni becomes difficult to reduce and becomes inactive.

  In view of this, a method has been proposed in which tar and char in a low temperature range are effectively prevented from being generated using a more active Rh or Ru-based catalyst (for example, Patent Documents 1 and 2).

JP 2003-246990 A JP-A-10-52639

  However, the above prior art is expensive because it uses a noble metal catalyst, and the running cost is inevitably increased when used as an industrial production scale and cannot be adopted.

  Therefore, in view of the above-described problems of the prior art, the object of the present invention is to have sulfur resistance and resistance even if the furnace is operated at a low temperature of 1000 ° C. or lower without using an expensive noble metal catalyst. An object of the present invention is to provide a method for producing a gasification catalyst and a gasification treatment system that exhibit coking properties, hardly dissolve Ni in solid solution, and yet exhibit high activity.

  The above-mentioned subject is achieved by the invention described in each claim. That is, the gasification catalyst according to the present invention is characterized by a gasification catalyst having a composite of one or more selected from nickel sulfate, nickel acetate, and nickel carbonate, and a magnesium raw material and a calcium raw material. The composite includes one or more of tungsten salt, cobalt salt, and molybdenum salt, and includes 5 to 30 wt% of nickel. The composite surface has one or more of tungsten, cobalt, and molybdenum components. Two or more types and the nickel component are highly dispersed.

  According to this configuration, one or more of the tungsten, cobalt, and molybdenum components and the nickel component and the nickel component can be dispersed in a high concentration on the surface as well as the inside of the composite. In the gasification of the system gasified product, even if the furnace temperature is about 500 to 900 ° C., the generation of char and tar can be effectively suppressed, and even if it is generated, it can be effectively decomposed. In particular, the tungsten, cobalt, and molybdenum components take in a sulfur component that is easily adsorbed by nickel, and when the catalyst according to the present invention is put into a gasification furnace, it acts to desorb into the gas, so the nickel catalytic activity is high. Maintained, and reliably and effectively suppresses sulfur poisoning of the catalyst. In addition, it is possible to effectively promote decomposition even for polycyclic aromatic tars such as naphthalene and phenanthrene, which have been difficult to suppress in the conventional technology. Can do. In addition, nickel sulfate, nickel acetate, and nickel carbonate can effectively suppress a decrease in specific surface area during firing due to sintering (crystallization) of magnesium oxide as compared with nickel nitrate, thereby enhancing catalytic activity.

In this way, even when gasifying organic gasified products such as biomass, the generation of char and tar is suppressed, so the carbon conversion efficiency increases, and when the generated gas is used for power generation facilities, the power generation efficiency When the generated gas is used for methanol or dimethyl ether, fuel conversion efficiency is increased. In addition, since gasification is promoted even when the H ₂ O / C ratio is as low as 1 to 3, when operating the gasification furnace, the amount of water vapor can be reduced and the sensible heat component by the introduction of water vapor can be reduced. It is possible to reduce the thermal loss. If the nickel content is less than 5 wt%, it is difficult to sufficiently exert the catalytic effect. Conversely, even if it is added in excess of 30 wt%, the increase in the effect is small for the amount, which is not preferable. Examples of the calcium raw material include dolomite, light-burned dolomite (dolomite baked at about 950 ° C. or higher), heavy-burned dolomite (dolomite baked at about 1300 ° C. or higher), slaked lime, and the like. In this specification, high dispersion means a state in which the entire surface of the composite is covered with a fine nickel component, tungsten, cobalt, or molybdenum component. When these nickel components are dispersed largely and roughly, carbon is deposited in the vicinity of the nickel components, hindering the tar decomposition reaction, and the deposited carbon causes the nickel components and the like to be separated from the catalyst surface, thereby deteriorating the catalyst performance. It becomes.

  As a result, even if the furnace is operated at a low temperature of 1000 ° C. or less without using an expensive precious metal catalyst, it exhibits sulfur resistance and coking resistance, Ni is hardly dissolved, and yet has high activity. The gasification catalyst which exhibits can be provided.

  It is preferable that the tungsten salt is ammonium tungstate, the cobalt salt is cobalt nitrate, cobalt sulfate, or cobalt acetate, and the molybdenum salt is ammonium molybdate.

  According to this configuration, it is possible to maintain a catalytic action with higher sulfur resistance and higher activity. Ammonium tungstate, cobalt nitrate or cobalt sulfate or cobalt acetate, and ammonium molybdate are preferably included in the catalyst product in an amount of 5 to 30 wt%, more preferably 5 to 15 wt% as each metal component (tungsten, cobalt, and molybdenum). Preferably, it contains 10 to 15 wt%. If it is less than 5 wt%, the sulfur resistance effect is not sufficient, and even if added in excess of 30 wt%, the increase in the effect is small for the amount added.

  Furthermore, aluminum oxide may be included. According to this configuration, the thermal stability of the catalyst can be improved without impairing the coking property. The amount of aluminum oxide added is 5-15 wt% aluminum. If the aluminum content is less than 5 wt%, the effect is poor.

  In addition, the characteristic configuration of the method for producing a gasification catalyst according to the present invention is that one or more of tungsten salt, cobalt salt, molybdenum salt, nickel sulfate, and magnesium oxide are mixed to cause a composite reaction. The composite material is dehydrated and washed, mixed with calcium raw material, then dried and fired.

  According to this configuration, even if the furnace is operated at a low temperature of 1000 ° C. or less without using an expensive noble metal-based catalyst, it exhibits sulfur resistance and coking resistance, and Ni is not easily dissolved. Nevertheless, a method for producing a gasification catalyst exhibiting high activity can be provided. In addition, compared with the case where nickel raw materials other than nickel sulfate (nitrate, acetate, carbonate, etc.) are used, the waste liquid treatment cost generated during cleaning can be reduced.

  Furthermore, as a characteristic constitution of the method for producing a gasification catalyst according to the present invention, one or more of tungsten salt, cobalt salt, molybdenum salt, nickel acetate, nickel carbonate and magnesium oxide are mixed to cause a composite reaction. And it is good also as a structure which mixes a calcium raw material with this, and is dried after that and baking.

  Even with this configuration, even if the inside of the furnace is operated at a low temperature of 1000 ° C. or less without using an expensive noble metal-based catalyst, it exhibits sulfur resistance and coking resistance, and Ni is hardly dissolved, and yet A method for producing a gasification catalyst exhibiting high activity can be provided. In addition, since nickel acetate or nickel carbonate is used, it is not necessary to dehydrate before adding the calcium raw material as in the case of using nickel sulfate, and the process can be simplified.

  It is preferable that the tungsten salt is ammonium tungstate, the cobalt salt is cobalt nitrate, cobalt sulfate, or cobalt acetate, and the molybdenum salt is ammonium molybdate.

  According to this configuration, it is possible to maintain a catalytic action with higher sulfur resistance and higher activity.

  It is preferable that the complexing reaction is performed at 45 to 90 ° C. and the baking is performed by heating to 500 to 900 ° C.

  According to this configuration, the complexing reaction can be efficiently generated. If the complexing reaction is less than 45 ° C., the progress of the complexing reaction is slow, and if it exceeds 90 ° C., a uniform complexing reaction is unlikely to occur.

  Furthermore, the gasification treatment system according to the present invention is characterized in that the gasification catalyst obtained by the above-described production method is introduced into a gasification furnace that heats and burns an organic gasification product. It is in that.

  According to this configuration, even if the furnace is operated at a low temperature of 1000 ° C. or less without using an expensive noble metal-based catalyst, it exhibits sulfur resistance and coking resistance, and Ni is not easily dissolved. In addition, a gasification processing system having a gasification catalyst exhibiting high activity can be provided. In addition, since the furnace temperature can be lowered, it is not necessary to use an expensive material as the furnace constituent material, and the manufacturing cost of the entire system can be reduced.

  It is preferable that a downstream side of the gasification furnace has a catalyst recovery device for recovering the introduced catalyst, and further has a tar decomposition facility for charging the catalyst downstream.

  According to this configuration, a small amount of tar that may remain after gasification can be reliably decomposed by the tar decomposition facility.

The schematic block diagram of the gasification processing system which concerns on one Embodiment of this invention. The flowchart which shows the manufacturing method of the catalyst of 1st Embodiment which concerns on this invention. The same flow chart as FIG. 2 showing the manufacturing method of the catalyst of the second embodiment The figure which shows the relationship between the tar alternative substance decomposition rate of each Example and a comparative example, and reaction temperature Each example shows the relationship between tar substitute material decomposition rate and the concentration of H ₂ S in the comparative example Each example shows the relationship between alternative material decomposition rate and the concentration of H ₂ S in the comparative example

  Embodiments of the present invention will be described in detail with reference to the drawings. FIG. 1 shows a schematic configuration of a gasification processing system according to the present embodiment.

  This gasification processing system includes a gasification furnace 1 to which fuel and air made of an organic material to be gasified such as biomass and oxygen and water vapor are supplied as needed, and a tar to be described later in the gasification furnace 1. Consists of a means for introducing a catalyst for suppressing the generation of components, a recovery device 2 for recovering the input catalyst, a dust collector 3 for removing dust in the generated gas as required, and a tar decomposition facility 4 Has been. The gas discharged from the tar decomposition facility 4 is further supplied to a power generation facility or various fuel conversion facilities (not shown) such as a downstream gas turbine or a gas engine, and is used as fuel.

  As described above, the gasification furnace 1 is supplied with a catalyst capable of effectively suppressing the generation of tar components even if the inside of the furnace is operated at a low temperature of 1000 ° C. or lower, in addition to biomass and combustion air. In addition, a cyclone 2 that is a catalyst recovery device is connected to the downstream side of the gasification furnace 1. However, the catalyst recovery device is not limited to a cyclone, and a ceramic filter or the like may be used.

  When a fluidized bed type furnace is used as the gasification furnace 1, the catalyst can be mixed into the fluidized medium. When other fixed bed type gasification furnaces are used, the catalyst is sprayed into the furnace. Can be used. In this way, since gasification is remarkably promoted, the generation of the tar content can be greatly suppressed even if the operation is performed at a furnace temperature of 1000 ° C. or lower. The temperature in the furnace that is actually operated may be about 500 to 900 ° C, and more preferably 700 to 850 ° C. A method for producing the catalyst supplied to the gasification furnace 1 will be described later.

  The tar decomposition facility 4 is for decomposing a small amount of tar that may remain after gasification, and is preferably provided after dust collection treatment on the rear stage side of the gasification furnace 1. However, the above catalyst is added to ensure the decomposition of tar content. The catalyst unit 4a of the tar decomposition facility 4 may be a fixed bed type or a fluidized bed type, and is heated to 500 to 900 ° C., more preferably 750 to 850 ° C. Disassemble.

  Next, a method for producing a catalyst used in the gasification furnace 1 will be described with reference to FIGS.

<First Embodiment>
As shown in FIG. 2, first, a predetermined amount of an aqueous solution of nickel sulfate, which is one of nickel salts, is prepared, and one or two or more aqueous solutions or suspensions selected from oxides of tungsten, cobalt, and molybdenum. After sufficiently mixing the turbid liquid or powder (# 1), a magnesium oxide powder or suspension is further added and mixed well to cause a composite reaction (# 2). In this case, the mixed solution is brought to 45 to 90 ° C., preferably 60 to 90 ° C., and subjected to a complexing reaction. If the temperature is lower than 45 ° C, the progress of the complexing reaction is slow. Nickel sulfate is blended so as to be 5 to 30 wt% of nickel in the catalyst. If nickel is less than 5 wt%, it is difficult to sufficiently exhibit the catalytic effect. Conversely, even if it is added in excess of 30 wt%, it is not preferable because it is laminated on the surface and the increase in the dispersion effect is small for the amount. Preferably, the nickel in the catalyst is 15-25 wt%.

  The composite slurry is filtered, dehydrated and washed to remove the generated sulfate ions (# 3). By removing the sulfuric acid component, it is possible to prevent the formation of calcium sulfate that inhibits the catalytic activity when the calcium raw material is added in the next step.

  After dehydration and washing, water is added to the mixture to add water, and dolomite such as light calcined dolomite, which is a calcium raw material, or slaked lime is added and mixed well to cause a complexing reaction (# 4). Dispersion of nickel and magnesium oxide is prevented by dispersing the calcium raw material in magnesium oxide. The calcium raw material is preferably added as calcium oxide in an amount of about 5 to 20 wt%, and more preferably about 7 to 12 wt%. When the calcium raw material exceeds 20 wt%, the uniform dispersibility of nickel becomes low. Also in this case, the mixed solution is subjected to a complexing reaction at 45 to 90 ° C., preferably 60 to 90 ° C.

  Then, it is dried and baked to evaporate water using a drying furnace or the like (# 5). The drying temperature is preferably about 80 to 120 ° C. However, it may be sprayed into a heated atmosphere by a spray drying method or the like and rapidly dried, and is not particularly limited to the drying method. By this treatment, a highly active catalyst can be generated (# 6). Firing is performed at 500 to 900 ° C., preferably about 700 ° C. The catalyst thus produced is finally pulverized to an appropriate size so as to be easily put into the gasification furnace, and the particle size is adjusted. Alternatively, it is molded (extruded, rolled, padlock, etc.) and formed into a shape that can be filled (pellets, rings, honeycombs, balls, etc.). When a composite of nickel, magnesium oxide and calcium oxide raw material is fired, the nickel can be prevented from excessively dissolving in the magnesium oxide, and the nickel can be highly dispersed on the surface of the magnesium oxide. The activity can be increased.

  When the calcium raw material is added after the hydration treatment, aluminum oxide may be added so that the aluminum content is 5 to 15 wt%. If it does in this way, thermal stability can be improved further, without impairing coking resistance.

Second Embodiment
Instead of nickel sulfate used in the first embodiment, nickel acetate or nickel carbonate is used. That is, as shown in FIG. 3, a predetermined amount of an aqueous solution of nickel acetate or nickel carbonate which is one kind of nickel salt is prepared, and one or more kinds selected from oxides of tungsten, cobalt and molybdenum. After the aqueous solution, suspension or powder is sufficiently mixed (# 1), further magnesium oxide powder or suspension is added and mixed well to cause a complexing reaction (# 2). Also in this case, nickel acetate or nickel carbonate is blended so as to be 5 to 30 wt% of nickel in the catalyst.

  Then, without dehydration and washing, dolomite such as light calcined dolomite, which is a calcium raw material, or slaked lime is added and mixed thoroughly to cause a complexing reaction (# 3). Also in this case, the mixed solution is brought to 45 to 90 ° C., preferably 60 to 90 ° C., to carry out a complexing reaction. The calcium raw material is dispersed in a compound such as nickel / magnesia, and the calcium raw material is preferably added in an amount of about 5 to 20 wt% as calcium oxide, as in the first embodiment.

  Next, it is filtered, dehydrated and washed (# 4), and then dried and baked to evaporate moisture using a drying furnace or the like (# 5). In that case, the drying temperature is about 80 to 120 ° C. This is the same as in the first embodiment. However, after adding the calcium raw material, the acetate may be removed by oxidation in the drying / firing step without dehydrating and washing. In this way, it is not necessary to perform waste liquid treatment including acetate ions, and the entire equipment cost and equipment space can be effectively reduced.

  By this treatment, a highly active catalyst can be generated (# 6). Firing is the same as in the first embodiment in that heating is performed at 500 to 900 ° C., preferably about 700 ° C. Moreover, when adding a calcium raw material, you may add an aluminum oxide so that an aluminum component may be 5-15 wt%. The same effect as described above can be exhibited.

  Hereinafter, the results of performance tests performed on the example catalyst manufactured by the manufacturing process shown in FIGS. 2 and 3 together with the comparative example catalyst will be described.

  First, the catalyst (Example 1) manufactured by the manufacturing process shown in FIG. 2 and a commercially available catalyst (Comparative Examples 1 to 6) were subjected to a comparative test by the following performance evaluation method.

[Performance evaluation method]
The performance evaluation method of the obtained catalyst was used as a substitute for tar using a toluene solution of naphthalene as a gas component having the composition shown in Table 1 according to the conditions shown in Table 1 and adjusting with a cylinder gas. The decomposition rate was measured by exposing to water. At that time, the tar substitute substance decomposition rate at a reaction temperature of 800 ° C. was measured for an H ₂ S concentration of 0 to 500 vol-ppm. The measurement results for the above examples are shown in FIGS.

(Example 1 (A))
According to the process shown in FIG. 2, nickel sulfate (nickel 20 wt%), a tungsten salt (using ammonium tungstate as an example. 10 wt% as a metal component), and a magnesium oxide suspension are added and mixed to form a composite. Then, after dehydrating and washing, the mixture was mixed with a light dolomite having a weight ratio of 7: 3, and the aqueous solution temperature was about 60 ° C. to cause a complexing reaction. This mixture was dried at 120 ° C., and the dried one was fired at about 500 ° C.

(Comparative Examples 1-6)
A commercially available steam reforming catalyst, Ni / Al ₂ O ₃ system with nickel supported on aluminum oxide (manufacturer: JGC Chemicals, trade name: N139, Comparative Example 1 (a)), nickel supported on aluminum oxide the Ni / Al ₂ O ₃ system (manufacturer: Süd-Chemie catalyst trade name:.. FCR-4 Comparative example 2 (b)), Ni / Al 2 O 3 · MgO · carrying nickel oxide aluminum oxide magnesium CaO system (manufacturer: Kyushu Fire Brick Company, trade name: DAN-N, Comparative Example 3 (c)), Ni / SiO ₂ system with nickel supported on silicon oxide (manufacturer: JGC Chemicals, trade name: N112) Comparative Example 4 (d)), Ru / Al ₂ O ₃ system with ruthenium supported on aluminum oxide (manufacturer: JGC Chemical Co., Ltd., trade name: E9R, Comparative Example 5 (e)), ruthenium supported on aluminum oxide Ru / Al ₂ O ₃ system (manufacturer: Sud Chemie Catalysts Inc., trade name: RUA, Comparative Example 6 (f)) was used.

From the results shown in FIGS. 4 and 5, the catalyst of Example 1 is excellent in low temperature activity, maintains high activity even in the presence of H ₂ S, and is excellent in coking resistance as compared with the catalysts of Comparative Examples. I understand that. In addition, C in FIG. 4 represents the point where coking was seen.

  Table 2 shows the results of measuring the carbon content and sulfur content of each catalyst of Example 1 and Comparative Example 5 after use as a catalyst (catalyst temperature: 800 ° C. × 10 hours). The carbon content is analyzed according to JIS M8819. The sulfur content is measured by boiling the catalyst in nitric acid and eluting the sulfur content, and then the filtrate is converted to JIS K0102III (turbidimetric method using barium sulfate). And analyzed.

  From the results in Table 2, it can be seen that the catalyst of Example 1 has less carbon and sulfur than the comparative example, and exhibits coking resistance and sulfur resistance.

Next, the catalyst (Examples 1 to 3) manufactured by the manufacturing process shown in FIGS. 2 and 3 and the catalyst using other nickel salts (Comparative Examples 7 and 8) were combined with H ₂ S at a catalyst temperature of 800 ° C. In order to compare the activity in the tar, the tar substitute substance decomposition rate is shown in FIG. 6 and the physical properties were evaluated by the following physical property evaluation methods.

[Physical property evaluation method]
As a physical property evaluation method of the obtained catalyst, the BET specific surface area and the metal (nickel) specific surface area were compared. The BET specific surface area is calculated from the adsorption isotherm of nitrogen gas, and the metal specific surface area is reduced at 298 K with hydrogen gas at 900 ° C. using a specific surface area measuring device (BELSORP-min II manufactured by Nippon Bell Co., Ltd.). The hydrogen gas adsorption isotherm was measured, and the degree of dispersion and specific surface area of nickel were calculated.

(Example 2 (B))
A catalyst was produced in the same manner as in Example 1 except that nickel acetate (nickel 20 wt%) was used in place of nickel sulfate, and that the steps shown in FIG.

(Example 3 (C))
In Example 2, a catalyst was produced in the same manner as in Example 2 except that after the complexing reaction, drying and firing were performed without dehydration and washing.

(Example 4 (D))
A catalyst was produced in the same manner as in Example 3 except that nickel carbonate (nickel 20 wt%) was used instead of nickel acetate and ammonium carbonate was added for dissolving nickel.

(Comparative Example 7 (h))
A catalyst was produced in the same manner as in Example 3 except that nickel nitrate (nickel 20 wt%) was used instead of nickel acetate.

  FIG. 6 shows the performance evaluation test results for each of the above examples, and Table 3 shows the physical property evaluation test results.

As shown in FIG. 6, at a catalyst temperature of 800 ° C., Examples 1-4 maintained the activity even in the presence of a high concentration of H ₂ S as compared with the catalyst of Comparative Example 7, and had a good tar decomposition rate. It can be seen that

  From the results in Table 3, it can be seen that the catalysts of Examples 1 to 4 have a larger specific surface area than the catalyst of Comparative Example 7, and the nickel component exhibits high dispersibility.

  As a result of the above, when sulfur content is included in the fuel, catalyst poisoning is likely to occur and the catalytic function is likely to deteriorate. The activity of desorbing is maintained, the activity of the nickel catalyst is maintained, and the catalyst poisoning is effectively suppressed. Therefore, according to the catalyst of this embodiment, tar content and the like can be effectively decomposed and removed at a low temperature range of 750 to 850 ° C. As a result, the carbon conversion rate is improved, and power generation efficiency (efficiency when gasified gas is used for power generation) and fuel conversion efficiency (efficiency when gasified gas is converted into methanol or dimethyl ether fuel) are improved.

[Another embodiment]
(1) As the gasification furnace, various types of furnaces such as a fluidized bed type, a fixed bed type, a kiln furnace, and a rotary furnace can be used and are not particularly limited.

1 Gasification furnace 2 Catalyst recovery device 4 Tar decomposition facility

Claims (6)

  Mixing one or more of tungsten salt, cobalt salt and molybdenum salt with nickel sulfate and magnesium oxide to cause a composite reaction, dehydrating and washing this composite, and mixing this with calcium raw material A method for producing a gasification catalyst which is then dried and calcined.   One or more of tungsten salt, cobalt salt, molybdenum salt and nickel acetate or nickel carbonate and magnesium oxide are mixed to cause a composite reaction, and then calcium raw material is mixed with this, followed by drying and firing. A method for producing a gasification catalyst.   The method for producing a gasification catalyst according to claim 1 or 2, wherein the tungsten salt is ammonium tungstate, the cobalt salt is cobalt nitrate, cobalt sulfate, or cobalt acetate, and the molybdenum salt is ammonium molybdate.   The method for producing a gasification catalyst according to claim 3, wherein the complexing reaction is performed at 45 to 90 ° C., and the calcination is performed by heating to 500 to 900 ° C.   The gasification catalyst obtained by the method for producing a gasification catalyst according to any one of claims 1 to 4 is introduced into a gasification furnace that heats and burns an organic gasification product to gasify it. Gasification processing system that has become.   It has the catalyst collection | recovery apparatus which collect | recovers the said introduced catalyst in the downstream of the said gasification furnace, and it is obtained with the manufacturing method of the gasification catalyst of any one of Claims 1-4 further downstream. The gasification processing system according to claim 5, further comprising a tar decomposition facility filled with a gasification catalyst.

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