JP4754844B2 - Method for producing desulfurizing agent for hydrocarbon fuel, desulfurizing agent for hydrocarbon fuel - Google Patents

Description

  The present invention relates to a method for producing a desulfurization agent for hydrocarbon fuels, a desulfurization agent for hydrocarbon fuels, a desulfurization method for hydrocarbon fuels, and a fuel cell system for removing sulfur compounds from hydrocarbon fuels. About.

  In order to supply hydrogen to a fuel cell, hydrogen is generally produced by a steam reforming reaction or the like using a catalyst for a hydrocarbon-based fuel that is a fuel gas in a reformer. However, since the catalyst in the reformer, particularly the steam reforming catalyst, is poisoned by the sulfur compound contained in the fuel, it is necessary to remove the sulfur content with a desulfurizing agent as a pretreatment.

  Among hydrocarbon fuels, city gas mainly composed of liquefied natural gas is added with sulfur compounds such as tertiary butyl mercaptan and dimethyl sulfide as an odorant. In this case, examples of the desulfurizing agent include a room temperature desulfurizing agent that is easy to handle.

  On the other hand, propane gas (LPG), kerosene, and the like among hydrocarbon fuels are promising fuels for fuel cells, and can be converted to hydrogen by a steam reforming catalyst. However, in the case of LPG, kerosene, etc., various sulfur compounds are contained depending on the production area and production method, and the concentration range is also various. In particular, it may contain carbonyl sulfide (COS), which is difficult to remove with a room temperature desulfurization agent. Therefore, in the case of hydrocarbon fuels such as LPG and kerosene, there is a problem that the room temperature desulfurization agent for city gas cannot sufficiently remove sulfur oxides.

  Therefore, desulfurization agents for hydrocarbon fuels that exhibit excellent desulfurization performance by heating the desulfurization agent to a high temperature have been studied. Examples of such desulfurization agents include nickel and copper on silica alumina carriers. A desulfurization agent (Patent Documents 1 and 2) in which iron is supported and a desulfurization agent (Patent Document 3) in which iron or nickel is supported on a mixture molded body of copper oxide and zinc oxide are known.

JP 2001-279271 A JP 2001-279260 A Japanese Patent Laid-Open No. 11-61154

  However, the desulfurization agents disclosed in Patent Documents 1 to 3 have a problem that the desulfurization activity is not yet sufficient from the low temperature range to the high temperature range.

  Therefore, in view of the above problems, the present invention provides a method for producing a desulfurization agent for hydrocarbon fuel and a desulfurization for hydrocarbon fuel that can sufficiently exhibit desulfurization activity from a low temperature region to a high temperature region. It is an object to provide an agent, a desulfurization method for hydrocarbon fuel, and a fuel cell system.

  The first invention of the present invention for solving the above-mentioned problem is that an aqueous solution of a precipitant kept at a predetermined temperature is mixed with at least one elemental compound of an aqueous solution containing Zn, Al or Cr, and oxidized. A step of generating a precipitate, a step of dropping an aqueous solution containing Cu and Ni into the oxidized precipitate to generate a composite oxide precipitate, and firing the obtained composite oxide precipitate to form a composite oxide A process for producing a desulfurizing agent for hydrocarbon fuels.

According to a second invention, in the first invention , the step of producing the oxidized precipitate further includes a firing step of firing the oxidized precipitate. A method for producing a desulfurizing agent for hydrocarbon fuel, It is in.

According to a third aspect of the present invention, there is provided a method for producing a desulfurization agent for a hydrocarbon fuel, which includes the step of reducing the desulfurization agent in the first or second aspect of the invention .

A fourth invention is the method for producing a desulfurization agent for hydrocarbon fuel, characterized in that, in the first invention , the aqueous precipitation agent solution is sodium carbonate or sodium hydrogen carbonate.

A fifth invention is a desulfurization agent for hydrocarbon fuel obtained by the method for producing a desulfurization agent for hydrocarbon fuel according to any one of the first to fourth aspects.

According to a sixth aspect of the present invention, there is provided a desulfurization method for hydrocarbon fuels, characterized in that the S content in the hydrocarbon fuel supplied to the fuel cell is removed using a desulfurization agent for the fifth hydrocarbon fuel. It is in.

A seventh invention is the desulfurization method for hydrocarbon fuel according to the sixth invention , characterized in that the desulfurization condition is normal temperature to 500 ° C.

The eighth invention includes a desulfurization apparatus having a desulfurization agent for a fifth hydrocarbon fuel, and after removing S in the hydrocarbon fuel supplied by the desulfurization apparatus, the hydrocarbon fuel desulfurized In a fuel cell system using a hydrocarbon fuel, the reformed gas is reformed by a reformer and the reformed gas is generated in a fuel cell.

A ninth invention is the fuel cell system according to the eighth invention , wherein the reformer includes a desulfurizer.

  According to the present invention, Cu is deposited with high dispersion around at least one elemental compound of an aqueous solution containing Zn, Al, or Cr by a two-stage treatment, so that it is high from a low temperature region to a high temperature region. Desulfurization activity is demonstrated.

  Hereinafter, the present invention will be described in detail with reference to the drawings. In addition, this invention is not limited by this embodiment and an Example. In addition, constituent elements in the following embodiments and examples include those that can be easily assumed by those skilled in the art or those that are substantially the same.

The method for producing a desulfurizing agent for hydrocarbon fuel according to an embodiment of the present invention includes at least one of a precipitant aqueous solution (eg, Na ₂ CO ₃ ) kept at a predetermined temperature and an aqueous solution containing Zn, Al, or Cr. And a step of producing an oxide precipitate and a step of dripping an aqueous solution containing Cu into the oxidation precipitate to produce a composite oxide containing Cu.
Further, for example, Ni may be supported on the composite oxide as an active component.

FIG. 1 shows an example of a first adjustment method of a desulfurization material for hydrocarbon fuel according to the present embodiment.
As shown in FIG. 1, first, as (Step 1), the solution A, which is a precipitant aqueous solution, is kept warm in the reaction vessel, and the aqueous solution B containing zinc (for example, Zn (NO ₃ ) ₂ ) is not stirred. It is dripped and a deposit is deposited to make it a suspended state.
Next, as a (step 2), a solution C containing copper (for example, Cu (NO ₃ ) ₂ ) is added dropwise to the suspension D (Zn (OH) CO ₃ ), and a precipitate E (Cu (OH) · CO 2 is added. ₃ , Zn (OH) · CO ₃ ).
Next, the precipitate E (Cu (OH) · CO ₃ , Zn (OH) · CO ₃ ) is washed with water and dried, and then fired to obtain an oxide (CuO—ZnO).
Nickel is supported on this oxide (CuO—ZnO) and molded into a predetermined shape to obtain a desulfurization agent. In addition, you may make it bake before carrying | supporting nickel.
Thus, by carrying out the precipitation treatment in two stages, zinc oxide becomes a nucleus, and particles having a form in which a composite oxide of copper and nickel is coordinated are formed around this.

Here, as the precipitant aqueous solution, Na ₂ CO ₃ is exemplified, but other examples include basic carbonate compounds such as NaHCO ₃ and K ₂ CO ₃ .

In this embodiment, Zn (NO ₃ ) ₂ is exemplified as the solution B, but complex oxidation is performed by simultaneously adding elements other than zinc, such as Al (NO ₃ ) ₃ , Cr (NO ₃ ) _{3, and the} like. You may make it form a thing.

Here, the ratio of Zn to Cu is 1: 0.1 to 5, preferably 1: 0.5 to 2, and more preferably 1: 0.7 to 1.5 (molar ratio).
The ratio of Al to Cu is 1: 0.01 to 2, preferably 1: 0.05 to 1, and more preferably 1: 0.1 to 0.5 (molar ratio).
Moreover, the ratio of Cr with respect to Cu is 1: 0.01-2, Preferably it is 1: 0.05-1, More preferably, it is 1: 0.1-0.5 (molar ratio).
Moreover, the ratio of Ni with respect to Cu is 1: 0.01-2, Preferably it is 1: 0.02-1, More preferably, it is 1: 0.05-0.5 (molar ratio).
Here, the reason why Cr is used as a component of the composite oxide is that it is a metal that serves as a nucleus for networking Cu and Zn, which makes it suitable as a composite oxide.

  In the above (Step 2), when the precipitate E is generated, the pH at the end of dropping is preferably adjusted to 4 or more. This is because when the pH is less than 4, all metal ions may not be precipitated as a composite oxide.

  Moreover, as for the baking conditions for baking the precipitate E after washing and drying, for example, baking is preferably performed at around 300 ° C.

  In addition, in the case of obtaining a solid-type desulfurization agent by pressure molding, the shape is not particularly limited. ).

  The desulfurization agent thus obtained has good desulfurization activity from the low temperature range to the high temperature range when removing S content in the raw fuel used in the fuel cell, as shown in the examples described later. Is.

Here, as the raw fuel used in the fuel cell desulfurized by the desulfurizing agent according to the present invention, for example, the fuel gas is C1 (compound containing one carbon, for example, CH ₄ ) to C12 (compound containing 12 carbons, For example, it contains one or more compounds selected from hydrocarbon gases composed of C ₁₂ H ₂₆ ). For example, the fuel gas is CH ₄ (methane), C ₂ H ₆ (ethane), C ₃ H ₈ (propane), C ₄ H ₁₀ (butane), C ₅ H ₁₂ (pentane), C ₆ H ₁₄ (hexane), C ₇ H ₁₆ (heptane), C ₈ H ₁₈ (octane), C ₉ H ₂₀ (nonane), C ₁₀ H ₂₂ (decane), C ₁₁ H ₂₄ , C One or more compounds selected from hydrocarbon gases composed of ₁₂ H ₂₆ are included. The fuel gas in the present invention widely includes so-called fossil fuels such as general city gas, LPG (liquefied petroleum gas), LNG (liquefied natural gas), methane gas, kerosene, and gasoline. The city gas in the present invention refers to a gaseous fuel supplied to an unspecified number of consumers through a conduit, and widely includes gases produced by modifying or mixing natural gas, crude oil, naphtha, coal, or the like. Although not intended to be limiting, city gas includes, as standard components, for example, about 70 wt.% To about 80 wt.% Methane, about 10 wt.% Ethane and about 10 wt.% Propane. Most of them contain 20% by weight or less and about 10% by weight or less of butane. The LPG (liquefied petroleum gas) in the present invention is a mixture of hydrocarbons such as propane and butane. The LPG (liquefied natural gas) in the present invention refers to a gas obtained by pressurizing and cooling natural gas mainly composed of methane.

Further, Al (NO ₃ ) ₃ and Cr (NO ₃ ) ₃ are simultaneously added to Zn (NO ₃ ) ₂ as solution B to form suspension D, and then solution C (Cu (NO ₃ ) ₂ ). dropwise to form a precipitate was E (Cu (OH) · CO 3 -Zn (OH) · CO 3 -Al (OH) · CO 3 -Cr (OH) · CO 3 and washed and dried the product After that, the desulfurization agent may be obtained by firing.

Further, nickel may be supported simultaneously in step 2.
FIG. 2 shows an example of a second adjustment method of the desulfurization material for hydrocarbon fuel according to the present embodiment.
As shown in FIG. 2, first, as (Step 1), the solution A, which is a precipitant aqueous solution, is kept warm in the reaction vessel and stirred, so an aqueous solution containing zinc (for example, Zn (NO ₃ ) ₂ ) is dropped. Then, the precipitate is deposited to be in a suspended state.
Next, as a (step 2), a solution C (for example, Cu (NO ₃ ) ₂ ) and a solution F (Ni (NO ₃ ) ₂ ) containing copper are added dropwise to the suspension D (Zn (OH) CO ₃ ). Thus, precipitates G (Ni (OH) · CO ₃ , Cu (OH) · CO ₃ , Zn (OH) · CO ₃ ) are produced.
Next, the precipitate G (Ni (OH) · CO ₃ , Cu (OH) · CO ₃ , Zn (OH) · CO ₃ ) is washed with water and dried, and then fired to obtain an oxide (NiO—CuO—ZnO). )
This oxide ((NiO—CuO—ZnO) is molded into a predetermined shape to obtain a desulfurization agent.
Thus, when precipitation is performed in two stages, Ni is also dropped at the same time, whereby zinc oxide serves as a nucleus, and a complex oxide of copper and nickel is coordinated in a highly dispersed state around this. Particles will be formed. Thus, since the solution C and the solution F are dripped simultaneously in the suspension D, it will be in the coexistence state of Cu and Ni with favorable dispersibility, and more Cu can be taken in. As a result, Cu becomes highly dispersed and Cu does not stick to each other, so that the desulfurization activity is further improved.

  The desulfurizing agent thus obtained has good desulfurization activity from the low temperature region to the high temperature region, as shown in the examples described later.

The dropping of nickel is not limited to the step shown in FIG. 2, and a nickel solution F may be dropped separately after steps 1 and 2 as shown in FIG.
FIG. 3 shows an example of a third adjustment method of the desulfurization material for hydrocarbon fuel according to the present embodiment.
As shown in FIG. 3, first, as (Step 1), the solution A, which is a precipitant aqueous solution, is kept warm in the reaction vessel, and the aqueous solution containing zinc (for example, Zn (NO ₃ ) ₂ ) is added dropwise without stirring. Then, the precipitate is deposited to be in a suspended state.
Next, as a (step 2), a solution C containing copper (for example, Cu (NO ₃ ) ₂ ) is added dropwise to the suspension D (Zn (OH) CO ₃ ), and a precipitate E (Cu (OH) · CO 2 is added. ₃ , Zn (OH) · CO ₃ ).
A solution F (Ni (NO ₃ ) ₂ ) is dropped into the suspension H containing the precipitate E, and the precipitate G (Ni (OH) · CO ₃ , Cu (OH) · CO ₃ , Zn (OH) · CO ₃ ) is produced.
Next, the precipitate G (Ni (OH) · CO ₃ , Cu (OH) · CO ₃ , Zn (OH) · CO ₃ ) is washed with water and dried, and then fired to obtain an oxide (NiO—CuO—ZnO). )
This oxide ((NiO—CuO—ZnO) is molded into a predetermined shape to obtain a desulfurization agent.
Thus, during the precipitation process in three stages, by dropping Ni at the end, the oxide of zinc becomes a nucleus, and copper is coordinated in a highly dispersed state around this, and coordinated in a highly dispersed state. Particles having a form in which nickel is arranged on copper are formed.
In addition, you may make it perform baking before precipitation of copper and nickel.

  The desulfurizing agent thus obtained has good desulfurization activity from the low temperature region to the high temperature region, as shown in the examples described later.

  Further, the obtained composite oxide may be further accelerated in the desulfurization reaction rate by subjecting nickel oxide to a reduction activation process of nickel oxide into nickel metal, for example.

Hereinafter, a power generation system of a fuel cell to which a desulfurization apparatus using the desulfurization agent of the present invention can be applied will be described with reference to the drawings.
FIG. 4 is a conceptual diagram showing a power generation system of a PEFC type fuel cell.
As shown in FIG. 4, a PEFC type fuel cell power generation system (PEFC power generation system) 1000 according to this embodiment includes a fuel electrode 1002-1 that supplies a fuel gas 1001, and an air electrode 1002-2 that supplies air 1003. The fuel cell 1002 including the cooling unit 1002-3 that supplies the refrigerant 1004 and removes the heat generated by the electrochemical reaction during operation, and the fuel gas 1001 supplied to the fuel electrode 1002-1 are modified from the raw fuel 1005. And a fuel reformer 1006 for generating the electric power, and the electric power is generated by the fuel supplied to the fuel electrode 1002-1 to obtain the DC power 1020 from the fuel cell 1002. This power generation system 1000 is configured to fully automatically start, generate, stop, and alarm / protect a fuel cell by a control system (not shown).

  Examples of the raw fuel 1005 by the reformer include gaseous fuels such as natural gas (city gas: 13A, for example) and LPG, and the main fuel 1005 is used to remove S components contained in the natural gas and LPG. A desulfurization apparatus 1007 using the desulfurization agent according to the invention is provided.

Here, the sulfur compound in the LPG includes dimethyl sulfide, methyl ethyl sulfide, tertiary butyl mercaptan, etc. (LPG1), dimethyl sulfide, methyl ethyl sulfide, tertiary butyl mercaptan, etc., as well as carbonyl sulfide. (COS) etc. contain (LPG2).
Further, the desulfurization temperature is preferably in the range from low temperature (−20 ° C.) to 500 ° C., more preferably from room temperature to 300 ° C.

  Further, as the desulfurization apparatus 1007, as shown in FIG. 5, the first desulfurization section 1007-1 and the second desulfurization section 1007-2 are arranged in two stages in series, and the first desulfurization section 1007-1 on the front stage side has For example, a room temperature desulfurization agent such as Ag / zeolite may be provided, and the second desulfurization part 1007-2 on the rear stage side may use the above-described desulfurization agent of normal temperature to high temperature (300 ° C.) according to the present invention. Thereby, the carbonyl sulfide (COS) derived from the raw material can be actively collected on the downstream side.

  Further, when the desulfurization device 1007 is provided independently or when used in a high temperature range, for example, it may be provided integrally within the fuel reformer 1006 so as to effectively use heat.

The raw fuel 1005 desulfurized by the desulfurizer 1007 is reformed by the fuel reformer 1006. Here, the reforming of the raw fuel 1005 is mainly performed by a steam reforming reaction in a reforming catalyst (not shown) of the reformer body 1006-1A of the fuel reformer 1006-1 of the fuel reformer 1006. Done. That is, the raw fuel 1005 and the steam 1009 are mixed and circulated through the reforming catalyst layer, and the reformer burner 1006-1B is used to perform the steam reforming reaction (when using city gas, for example, at a temperature of 700 to 800 ° C. Is performed by causing CH ₄ + H ₂ O → CO + 3H ₂ ). Examples of the reforming catalyst include Ru / Al ₂ O _3, but are not limited thereto. Further, the reformed fuel gas 1001 may pass through a CO shift catalyst unit 1006-2 and a PROx (Preferential Oxidation) catalyst unit 1006-3 as necessary.

  The cooling line L1 of the refrigerant 1004 is provided with a heat radiating portion 1010 that exchanges heat, for example, water or air, and radiates heat when heat is generated in the fuel cell power generation. In the present system, various heat sources such as the heat radiating portion 1010 are used by utilizing heat generated accompanying the fuel cell reaction.

  In the system shown in FIG. 4, when fuel cell power generation is started, the raw fuel 1005 is supplied to the reformer burner 1006-1B to raise the temperature of the reformer body 1006-1A, which is suitable for steam reforming. After the predetermined temperature condition is satisfied, the raw fuel 1005 is supplied to reform the fuel gas 1001. Thereafter, the obtained fuel gas 1001 is further reformed as necessary, and then supplied to the fuel electrode 1002-1 to start power generation. The exhaust gas from the fuel electrode 1002-1 is sent to the reformer burner 1006-1B and burned there to use unreacted gas.

  Since the power generation system of the present PEFC type fuel cell performs desulfurization with the desulfurization apparatus 1007 using the above-described desulfurization agent for hydrocarbon fuel, stable desulfurization can be performed from a low temperature region to a high temperature region over a long period of time. And a highly reliable fuel cell system can be provided.

  Examples of the present invention will be described below, but the present invention is not limited to the following examples.

[Example 1]
Sodium carbonate (Na ₂ CO ₃ 2.5 mol) is dissolved in ₂ L of water and kept at 70 ° C. This alkaline aqueous solution is designated as Solution B. Next, 0.225 mol of zinc nitrate (Zn (NO ₃ ) ₂ .6H ₂ O and 0.075 mol of aluminum nitrate (Al (NO ₃ ) ₃ .9H ₂ 0) were dissolved in 400 cc of water and kept at 70 ° C., and this acidity The solution is defined as solution A. Further, 0.3 mol of copper nitrate (Cu (NO ₃ ) ₃ .3H ₂ 0) is dissolved in 200 cc of water and kept at 70 ° C., and this acidic solution is defined as solution C.

First, the solution B is uniformly added dropwise to the solution A over 30 minutes with stirring to obtain a suspension D. After the solution B is added dropwise, the solution C is added dropwise to the suspension over 30 minutes to obtain a precipitate G. The pH after completion of dropping was pH 7. Aging was performed for 1 hour after the dropping.
Next, the precipitate G is filtered and washed so that NO ₃ ions and Na ions are not detected. Furthermore, it was dried at 100 ° C. for 24 hours, and then fired at 300 ° C. for 3 hours to obtain a CuO—ZnO—Al ₂ O ₃ composite oxide.

2% by weight of graphite carbon was added to the composite oxide to form a cylindrical pellet of 3 mmφ × 3 mmL.
This pellet-shaped composite oxide was immersed in an aqueous nickel nitrate solution, evaporated to dryness with stirring to volatilize water, dried, and then fired at 300 ° C. for 3 hours. At this time, the amount of NiO supported was 5% by weight. This catalyst is designated as desulfurizing agent 1.

[Example 2]
In the preparation method of Example 1 above, in the CuO—ZnO—Al ₂ O ₃ composite oxide powder, this powder was impregnated and supported with an aqueous nickel nitrate solution, and after drying and firing, NiO was 5 wt% based on the whole. Supported.
In the same manner as in Example 1, this powder was formed into a cylindrical pellet. This pellet is designated as desulfurizing agent 2.

[Example 3]
Moreover, in the preparation method of Example 1, the nickel nitrate aqueous solution was added with respect to the copper nitrate aqueous solution of the solution C, and the mixed aqueous solution I of copper and nickel was obtained.
Thereafter, in the same manner as in Example 1, solution B was added to solution A to obtain a suspension, and then solution I was added dropwise to obtain a precipitate. This precipitate was filtered, washed with water, dried and fired in the same manner as in Example 1 and then molded into a cylindrical pellet. This pellet is designated as desulfurizing agent 3.

[Example 4]
Furthermore, in the preparation method of Example 1 above, 0.075 mol of chromium nitrate (Cr (NO ₃ ) ₃ .9H ₂ O) was added instead of aluminum nitrate in Solution A, and in the same method as in Example 1, A pellet molding desulfurization agent was prepared. This desulfurizing agent is designated as desulfurizing agent 4.

[Example 5]
Further, in the preparation method of Example 1 above, CuO—ZnO composite oxide was made without adding aluminum to the solution A, and a pellet molding desulfurization agent supporting NiO was prepared in the same manner as in Example 1. . This desulfurizing agent is designated as desulfurizing agent 5.

[Example 6]
Further, in the preparation method of Example 1 above, CuO—ZnO—Al ₂ O obtained by adding 0.075 mol of chromium nitrate (Cr (NO ₃ ) ₃ .9H ₂ O) together with the aluminum nitrate of Solution A _It was molded into a _3- Cr ₂ O ₃ composite oxide cylindrical pellet. This pellet is designated as desulfurizing agent 6.

  In addition, all the composite hydroxides of the desulfurizing agents 1 to 6 had a basic carbonate complex compound and had a hydrotalcite structure.

[Comparative Example 1]
Comparative desulfurization in which 51.0 wt% of Ni, 19.8 wt% of Cu and 4.9 wt% of Zn were supported on the silica-alumina support Si / Al molar ratio 5) based on the total amount of the desulfurizing agent according to Example 1 of Patent Document 2. Agent powder 1 was obtained. The obtained desulfurizing agent powder was molded into a cylindrical shape of 3 mmφ × 3 mmL to obtain a comparative solid desulfurizing agent 1.

[Comparative Example 2]
According to Example 1 of Patent Document 3, a comparative desulfurization catalyst powder 2 in which 5 wt% Ni was supported on Cu—Zn was obtained. Then, the obtained desulfurizing agent powder was molded into a 3 mmφ × 3 mmL cylindrical shape to obtain a comparative solid desulfurizing agent 2.

[Comparative Example 3]
According to Example 1 of Patent Document 3, a comparative desulfurization catalyst powder 3 in which 10 wt% Ni was supported on Cu—Zn was obtained. Then, the obtained desulfurizing agent powder was molded into a 3 mmφ × 3 mmL cylindrical shape to obtain a comparative solid desulfurizing agent 3.

[Testing method for desulfurization agent]
A desulfurization test using LPG was performed on the obtained solid desulfurization agents 1 to 6 and comparative solid desulfurization agents 1 to 3. Test conditions are listed in Table 1. During the test, after sampling the gas before and after the flow of the desulfurizing agent packed in the reaction tube, measuring the S concentration in the gas by gas chromatography, calculate the amount of S adsorbed on the catalyst until the S component slips at the catalyst outlet did.
As a pretreatment for any of the desulfurizing agents, pretreatment (reduction treatment) was carried out at 200 ° C. in a 3% H ₂ / N ₂ ] balance for 15 hours to convert the active metal from NiO to Ni.
Table 1 below shows the desulfurization performance evaluation conditions in this example. Table 2 shows the specifications and desulfurization performance of the desulfurizing agent.

  The results are shown in Table 2. As for the solid catalysts 1 to 5 according to Examples 1 to 6, the comparative solid catalysts 1 to 3 of Comparative Examples 1 to 3 were obtained at reaction tube inlet temperatures of 25 ° C. and 200 ° C. It is possible to remove S content in LPG.

  As described above, in the desulfurization agent for hydrocarbon fuel according to the present invention, Cu is deposited with high dispersion around at least one elemental compound of an aqueous solution containing Zn, Al, or Cr by a two-stage treatment. Therefore, it exhibits high desulfurization activity from the low temperature range to the high temperature range, and is suitable for use in the removal of the S content of the raw fuel of the fuel cell system.

It is process schematic of the 1st adjustment method concerning an embodiment. It is process schematic of the 2nd adjustment method concerning embodiment. It is process schematic of the 3rd adjustment method concerning embodiment. 1 is a schematic configuration diagram of a power generation system of a PEFC type fuel cell according to an embodiment. It is the schematic of the desulfurization apparatus concerning embodiment.

1000 PEFC type fuel cell power generation system 1001 Fuel gas 1002 Fuel cell 1002-1 Fuel electrode 1002-2 Air electrode 1002-3 Cooling unit 1003 Air 1004 Refrigerant 1005 Raw fuel 1006 Fuel reformer 1007 Desulfurization device

Claims (9)

A step of mixing an aqueous precipitant solution kept at a predetermined temperature with at least one elemental compound of an aqueous solution containing Zn, Al or Cr to produce an oxidized precipitate;
Dropping an aqueous solution containing Cu and Ni into the oxidation precipitate to form a composite oxide precipitate;
A method for producing a desulfurization agent for hydrocarbon fuels, comprising: calcining the obtained complex oxide precipitate to form a complex oxide. In claim 1 ,
The method for producing a desulfurizing agent for hydrocarbon fuel, wherein the step of generating the oxidized precipitate further includes a firing step of firing the oxidized precipitate. In claim 1 or 2 ,
A method for producing a desulfurizing agent for hydrocarbon fuel, comprising a step of reducing the desulfurizing agent. In claim 1 ,
The method for producing a desulfurization agent for hydrocarbon fuel, wherein the aqueous precipitant solution is sodium carbonate or sodium hydrogen carbonate. A desulfurization agent for hydrocarbon fuel obtained by the method for producing a desulfurization agent for hydrocarbon fuel according to any one of claims 1 to 4 . A desulfurization method for hydrocarbon fuel, wherein the sulfur content in the hydrocarbon fuel supplied to the fuel cell is removed using the desulfurization agent for hydrocarbon fuel according to claim 5 . In claim 6 ,
A desulfurization method for hydrocarbon fuel, characterized in that the desulfurization condition is normal temperature to 500 ° C. 6. A desulfurization apparatus having a desulfurization agent for hydrocarbon fuel according to claim 5 , wherein after removing S content in the hydrocarbon fuel supplied by the desulfurization apparatus, the desulfurized hydrocarbon fuel is removed by a reformer. A fuel cell system using a hydrocarbon-based fuel, wherein the reformed gas is reformed and power is generated in the fuel cell. In claim 8 ,
A fuel cell system comprising a desulfurization device in the reformer.

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