JP2002241774A - Apparatus and method for producing gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To decrease energy to be charged for progressing a reaction when producing a useful gas. SOLUTION: The apparatus for producing the gas comprises a reaction column 1 forming a passage 2 of a gaseous reactant, a solid catalyst 4 arranged in the passage 2, a first electrode 3 and a second electrode 5 which is a counter electrode of the first electrode 3. The first electrode 3 together with the second electrode 5 generates low-temperature plasma at the vicinity of the surface of the solid catalyst 4, and the Low-temperature plasma produces a product material by exciting the gaseous reactant. The same material as the solid catalyst used when producing the product material without using the plasma is used as the solid catalyst. The first electrode 3 is arranged on the wall in the inside of the reaction column 1, and the second electrode 5 has a rod shape and arranged at the center of the passage 2. The solid catalyst 4 is covered with the first electrode 3.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas producing apparatus and a gas producing method, and more particularly, to a gas producing apparatus and a gas producing method which require less input energy.

[0002]

_2. Description of the Related Art In the production of synthesis gas (CO + H ₂ ), steam and steam are reformed by utilizing a catalytic reaction in a high-temperature (about 750 to 850 ° C.) and high-pressure (about 20 atm) system. Method is used.

As shown in FIG. 3, a known synthesis gas production apparatus includes a desulfurization tower 101, a heater 102, a catalytic reaction tower 103, a carbon dioxide absorption tower 104, a carbon monoxide removal apparatus 105, and an absorbent regeneration tower. 106. The raw material hydrocarbon is supplied to the desulfurization tower 101 and is desulfurized. The desulfurized hydrocarbon is mixed with steam and supplied to the heater 102 to be heated. The mixed gas of the heated hydrocarbon and steam is supplied to the catalytic reaction tower 103 in which a steam reforming reaction occurs.

In the catalytic reaction tower 103, 750 to 850
℃, 20 atm, metal Ni catalyst supported on alumina carrier
The following chemical reaction proceeds in the system. CH₄+ H₂O → CO + 3H₂  CO + H₂O → CO₂+ H₂

The generated mixed gas of carbon monoxide, carbon dioxide and water vapor is supplied to a carbon dioxide absorption tower 104. The carbon dioxide absorption tower 104 is filled with an absorbing liquid that absorbs carbon dioxide, and removes carbon dioxide from the mixed gas. The mixed gas from which carbon dioxide has been removed is supplied to a carbon monoxide removing device 105, where carbon monoxide is removed and hydrogen is purified.

[0006] The carbon dioxide absorbing liquid that has absorbed the carbon dioxide is supplied to the absorbing liquid regeneration tower 106 to remove the carbon dioxide. The carbon dioxide absorbing liquid from which carbon dioxide has been removed is supplied to the carbon dioxide absorbing tower 104 again.

[0007] Hydrogen is produced by a water gas transfer reaction in which a synthesis gas is produced from a hydrocarbon and steam using a steam reforming method, and carbon monoxide contained in the synthesis gas is reacted with steam.

FIG. 4 shows the hydrogen production apparatus.
The raw material hydrocarbon is supplied to the desulfurization tower 101,
Is done. The desulfurized hydrocarbon and steam are supplied to the heater 10
2 and heated. Heated hydrocarbons and steam
The gas mixture is used as a catalyst in a catalytic reaction tower 1 that causes a steam reforming reaction.
03. In the catalyst reaction tower 103, 750 to 8
50 ° C., 20 atm, metal Ni supported on alumina carrier
The following reaction proceeds in the catalyst system. CH₄+ H₂O → CO + 3H₂  CO + H₂O → CO₂+ H₂

[0009] The generated mixed gas of carbon monoxide, carbon dioxide and water vapor is supplied to a catalytic reaction tower 114 which causes a water gas transfer reaction. In the catalyst reaction tower 114, 350 to
The following reaction proceeds in a system of a metal Fe + Cr catalyst supported on an alumina carrier at 400 ° C. CO + H ₂ O → CO ₂ + H ₂

The generated mixed gas is supplied to a carbon dioxide absorption tower 104. The carbon dioxide absorption tower 104 is filled with an absorbing liquid that absorbs carbon dioxide, and removes carbon dioxide from the mixed gas. The mixed gas from which carbon dioxide has been removed is supplied to a carbon monoxide removing device 105, where hydrogen is purified.

The carbon dioxide-absorbing liquid that has absorbed the carbon dioxide is supplied to an absorbing liquid regenerating tower 106 to remove the carbon dioxide. The carbon dioxide absorbing liquid from which carbon dioxide has been removed is supplied to the carbon dioxide absorbing tower 104 again. Such a water gas transfer reaction utilizes a high-temperature (about 300 to 500 ° C.) catalytic reaction and consumes a large amount of energy.

Ammonia reacts hydrocarbons with air (atmosphere) to produce synthesis gas containing nitrogen,
It is manufactured by performing a catalytic reaction in a high-pressure (about 100 to 1000 atm) system (50 to 550 ° C) (Haber-Bosch method).

FIG. 5 shows a known ammonia producing apparatus.
ing. The raw material hydrocarbon is supplied to the desulfurization tower 201.
And desulfurized. Desulfurized hydrocarbons and air (atmosphere)
Is supplied to the heater 202 and heated. Heated
The mixed gas of hydrocarbon and air is supplied to the catalytic reaction tower 203.
Is done. In the catalyst reaction tower 203, 450-550 ° C, 1
100-1000 atm, alumina carrier Fe-K₂O catalyst
The following reaction proceeds in the system. 2CH₄+ O₂→ 2CO + 4H₂  Further, a chemical equilibrium state represented by the following two equations is obtained. 3H₂+ N₂→ 2NH₃(Liquid) 2NH₃(Liquid) → 3H₂+ N₂  Hydrogen and nitrogen are supplied, and the generated liquid ammonia
As a result of the removal, the chemical equilibrium state
Proceed in the direction of formation.

Methane is obtained by converting syngas (CO + H ₂ ) into Rh, Ni (+ Th) at high temperature (about 250 to 500 ° C.) and normal pressure.
A method utilizing an O ₂ , MgO) catalytic reaction is used. Methane is produced by a useful gas producing apparatus as shown in FIG. A mixed gas as a raw material is supplied to a heater 30.
2 and heated. The heated mixed gas is supplied to the catalyst reaction tower 303. In the catalyst reaction tower 303,
250-500 ° C., normal pressure, Rh, Ni (+ ThO ₂ , M
gO) The following reaction proceeds in the catalyst system. CO + 3H ₂ → CH ₄ + H ₂ O

Paraffins and olefins can be obtained by synthesizing syngas at high temperature (150-350 ° C.) and high pressure (1-30 atm).
e, Cr, Ni) + ThO ₂ , HgO, alumina, K ₂
O) A method utilizing a catalytic reaction is used. Paraffin and olefin are produced by a useful gas producing apparatus as shown in FIG. The mixed gas as a raw material is supplied to the heater 302 and heated. The heated mixed gas is supplied to the catalyst reaction tower 303. Catalyst reaction tower 303
Then, 150 to 350 ° C. and 1 to 30 atmospheres, (Fe, Cr,
The following reaction proceeds in the system of Ni) + ThO ₂ , HgO, alumina, K ₂ O) catalyst. _{nCO + (2n + 1) H} 2 → C n H 2n + 2 + nH 2 O nCO + 2nH 2 → C n H 2n + nH 2 O

Methanol converts the synthesis gas to a high temperature (250 to
400 ° C) at high pressure (100-1000 atm) (ZnO +
A method utilizing a Cr ₂ O ₃ or ZnO + Cu + Al ₂ O ₃ ) catalytic reaction is used. Methanol is produced by a useful gas producing apparatus as shown in FIG. The mixed gas as a raw material is supplied to the heater 302 and heated. The heated mixed gas is supplied to the catalyst reaction tower 303.
Supplied to In the catalyst reaction tower 303, 250 to 400
° C. 100 to 1000 atm, the following reaction (ZnO + _Cr 2 _{O 3} or _{ZnO + Cu + Al 2 O 3} ) catalyst system proceeds. CO + 2H ₂ → CH ₃ OH

Ethanol converts syngas to high temperatures (about 300
C) at a high pressure (about 70 atm) using a (Rh, Fe) + SiO ₂ catalytic reaction. Ethanol is produced by a useful gas producing apparatus as shown in FIG. The mixed gas as a raw material is supplied to the heater 302 and heated. The heated mixed gas is supplied to the catalytic reaction tower 3
03. In the catalyst reaction tower 303, about 300 ° C.
The following reaction proceeds in a (Rh, Fe) + SiO ₂ catalyst system at about 70 atm. 2CO + 4H ₂ → C ₂ H ₅ OH + H ₂ O

Higher alcohols use a high temperature (about 3
00-450 ° C) ZnO at high pressure (100-400 atm)
A method utilizing + Cr ₂ O ₃ or ZnO + Cu + alkali catalyst reaction is used. The higher alcohol is produced by a useful gas producing apparatus as shown in FIG. The mixed gas as a raw material is supplied to the heater 302 and heated. The heated mixed gas is supplied to the catalyst reaction tower 303.
Supplied to In the catalyst reaction tower 303, 300 to 450
100 ° -400 atm, ZnO + Cr ₂ O ₃ or Zn
The following reaction proceeds in a system of O + Cu + alkali catalyst. _{nCO + 4nH 2 → C n H} 2n + 1 OH + (n-1) H
₂ O

[0019] Ethylene glycol is obtained by synthesizing syngas at high temperature (220-250 ° C) and high pressure (14000 atm) with Rh
A method utilizing a K, Ce salt catalyst reaction is used.
Ethylene glycol is produced by a useful gas producing apparatus as shown in FIG. The mixed gas as a raw material is supplied to the heater 302 and heated. The heated mixed gas is supplied to the catalyst reaction tower 303. Catalytic reaction tower 30
In No. 3, 220-250 ° C., 14000 atm, Rh + K,
The following reaction proceeds in the Ce salt catalyst system. 2CO + 3H ₂ → HOCH ₂ CH ₂ OH

In the low-temperature plasma, only some of the electrons acquire extremely high energy, only the electron temperature is extremely high, and the low-temperature plasma can be operated at normal temperature and normal pressure. Decomposition of harmful gases by a catalytic reaction using low-temperature plasma is known.

FIG. 7 shows a known low-temperature plasma reaction reactor. The reactor 400 is a packed bed reactor, and includes an AC power supply 404 and an external electrode 4.
01, an internal electrode 402, and a ceramic pellet 403, which is a ferroelectric substance, filled between the external electrode 401 and the internal electrode 402.

When the AC power supply 404 applies a high voltage between the external electrode 401 and the internal electrode 402, the pellet 403
The micro-discharge of nanosecond order is generated in the voids, and is turned into plasma. The harmful air pollutants (hereinafter, abbreviated as “HAPs”) in the target gas are decomposed by the plasma chemical reaction through the target gas into the gap.

Such a reactor 400 is not used for producing useful gases exemplified by synthesis gas, hydrogen, ammonia, methane, paraffin, olefin, methanol, ethanol, higher alcohol, and ethylene glycol.

[0024]

SUMMARY OF THE INVENTION It is an object of the present invention to provide a gas producing apparatus and a gas producing method which reduce the energy input for promoting the reaction.
Another object of the present invention is to provide a small-scale gas production apparatus and a gas production method.

[0025]

Means for solving the problem are described as follows. The technical items appearing in the expression are appended with numbers, symbols, etc. in parentheses (). The numbers, symbols, and the like are technical items that constitute at least one embodiment or a plurality of the embodiments of the present invention, in particular, the embodiments or the examples. Corresponds to the reference numerals, reference symbols, and the like assigned to the technical matters expressed in the drawings corresponding to the above. Such reference numbers and reference symbols clarify the correspondence and bridging between the technical matters described in the claims and the technical matters of the embodiments or examples. Such correspondence / bridge does not mean that the technical matters described in the claims are interpreted as being limited to the technical matters of the embodiments or the examples.

In the gas producing apparatus according to the present invention, a reaction tower (1, 21) forming a flow path (2, 22) for a gaseous reactant is provided.
And a catalyst (4, 24) disposed in the flow path (2, 22)
, A first electrode (3, 23), and a second electrode (5, 25) which is a counter electrode of the first electrode (3, 23). , 25), the low-temperature plasma generated near the surface of the catalyst based on the voltage applied between them excites the gaseous reactant to produce a product. The catalyst (4, 24) uses the same material as the catalyst (4, 24) used when generating a product without using plasma. By using such a catalyst (4, 24), a product is selected and generated from gaseous reactants, and the yield is improved.

The first electrode (3, 23) is connected to the reaction tower (1, 2).
Placed on the inner wall of 1), the second electrode (5, 25)
The catalyst (4, 24) is disposed in the channel (2, 22), and is covered with the second electrode (5, 25). Such an arrangement ensures that a low-temperature plasma is generated near the surface of the catalyst (4, 24).

The catalyst (4, 24) is preferably granular and filled in the flow path (2, 22) in that the contact area with the gaseous reactant is large. The catalyst (4, 24)
Flowable. Such a catalyst (4, 24) flows by blowing a gaseous reactant into the flow path (2, 22) to form a fluidized bed. There is an advantage that the reaction temperature is kept uniform by the heat transfer property of the fluidized bed, and the reaction heat is advantageous for a large reaction. Since the catalyst (4, 24) can be continuously extracted and replenished, it is convenient when the activity is rapidly deteriorated due to by-products and regeneration is required.

Preferably, the gaseous reactant is synthesis gas, the product is methane, and the catalyst (4,24) is rhodium, nickel, thorium oxide or magnesium oxide.

The gaseous reactant is a synthesis gas and the product is a paraffin or an olefin, which is a catalyst (4,2).
4) is preferably metal iron, metal cobalt, metal nickel, thorium oxide, magnesium oxide, alumina, or potassium oxide.

Preferably, the gaseous reactant is synthesis gas, the product is methanol and the catalyst (4,24) is zinc oxide, chromium oxide, zinc oxide, metallic copper or alumina.

Preferably, the gaseous reactant is a synthesis gas, the product is ethanol, and the catalyst (4,24) is a metal rhodium, metal iron or silica.

Preferably, the gaseous reactant is a synthesis gas, the product is a higher alcohol, and the catalyst (4,24) is zinc oxide, chromium oxide, zinc oxide, metallic copper, or an alkali metal. .

The gaseous reactant is synthesis gas, the product is ethylene glycol and the catalyst (4,24) is
Preferably, the metal is rhodium, metal potassium, or cerium.

The gaseous reactants are hydrocarbons and water vapor, the product is a synthesis gas, and the catalyst (4,24)
Is preferably metallic nickel supported on alumina.

The gaseous reactants are carbon monoxide and water vapor, the product is hydrogen, and the catalyst (4,24) is
It is preferably metallic iron or metallic nickel.

The gaseous reactant is a mixture of hydrocarbon and nitrogen, the product is ammonia, and the catalyst (4,
24) is preferably metallic iron, alumina or potassium oxide.

The fuel cell according to the present invention comprises a reaction tower (1, 21) forming a flow path (2, 22) of a gaseous reactant in which a hydrocarbon and water vapor are mixed, and a flow path (2, 22). A catalyst (4,24) disposed of metallic nickel, alumina, metallic iron or metallic chromium, and a first electrode (3,23)
And a second electrode (5, 5) which is a counter electrode of the first electrode (3, 23).
25) and a fuel cell main body, and the first electrodes (3, 2).
3) a catalyst (4, 24) together with a second electrode (5, 25)
A low-temperature plasma is generated on the surface of the fuel cell, and the low-temperature plasma excites a gaseous reactant to generate hydrogen.

Fuel cell bodies that generate electric power from hydrogen and oxygen are known. The oxygen mixture gas is preferably ambient air. Such a fuel cell does not need to supply hydrogen directly and is easy to handle.

The gas production method according to the present invention includes exciting a gaseous reactant with low-temperature plasma, causing a catalyst (4, 24) to act on the gaseous reactant, and producing a product from the gaseous reactant. . The low temperature plasma excites the gaseous reactant to produce a product. Catalyst (4
24) uses the same material as the catalyst (4, 24) used when generating a product without using plasma. By using such a catalyst (4,24), a product is selected and generated from the gaseous reactants,
In addition, the yield is improved.

And supplying thermal energy to the gaseous reactant with the low temperature plasma. If the chemical reaction that produces the product from the gaseous reactant involves an endothermic reaction, the low temperature plasma supplies the heat of reaction.

Preferably, the gaseous reactant is a synthesis gas, the product is methane, and the catalyst (4,24) is rhodium, nickel, thorium oxide, magnesium oxide.

The gaseous reactant is synthesis gas, the product is paraffin olefin, and the catalyst (4,24) is metallic iron, metallic cobalt, metallic nickel, thorium oxide,
It is preferably magnesium oxide, alumina, or potassium oxide.

Preferably, the gaseous reactant is synthesis gas, the product is methanol and the catalyst (4,24) is zinc oxide, chromium oxide, metallic copper or alumina.

Preferably, the gaseous reactant is synthesis gas, the product is ethanol, and the catalyst (4,24) is rhodium, metallic iron or silica.

Preferably, the gaseous reactant is a synthesis gas, the product is a higher alcohol, and the catalyst (4,24) is zinc oxide, chromium oxide, metallic copper, or an alkali metal.

Preferably, the gaseous reactant is synthesis gas, the product is ethylene glycol and the catalyst (4,24) is rhodium metal, potassium metal or cerium.

Preferably, the gaseous reactants are hydrocarbons and water vapor, the product is a synthesis gas, and the catalyst (4, 24) is metallic nickel supported on alumina.

Preferably, the gaseous reactants are carbon monoxide and water vapor, the product is hydrogen and the catalyst (4,24) is metallic iron or metallic nickel.

The gaseous reactant is a mixture of hydrocarbon and nitrogen, the product is ammonia, and the catalyst (4,2
4) is preferably metallic iron, alumina or potassium oxide.

[0051]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of a gas producing apparatus according to the present invention will be described with reference to the drawings. In the gas producing apparatus 10, as shown in FIG. 1, a chamber 1 forms a reaction gas flow path 2. The flow path 2 is parallel to the vertical direction, and the reaction gas flows vertically downward. Chamber 1
The electrode 3 is formed on the inner wall of the device and is grounded. The chamber 1 is formed of a conductor, and the electrodes 3
It may be shared. On the inner wall of the electrode 3, a catalyst layer 4 coated with a solid catalyst is formed.

The gas producing apparatus 10 has the electrode 5. The electrode 5 has a rod shape and is arranged in the center of the flow channel 2 so as to extend in the vertical direction. The electrode 5 is fixed while being electrically insulated from the electrode 3. The upper end of the chamber 1 is closed, and a reaction gas inlet 6 is provided on the upper wall of the chamber 1. The gas production device 10 further includes a high-voltage power supply 11. The high voltage power supply 11
A high voltage is applied between the electrode and the electrode 5 to generate low-temperature plasma.

The embodiment of the gas producing method according to the present invention includes flowing a reaction gas at normal temperature and normal pressure from the inlet 6 and applying a high voltage to the electrodes 3 and 5. First, a reaction gas is passed from the inlet 6 to the flow channel 2. Thereafter, when the high-voltage power supply 11 applies a high voltage to the electrodes 3 and 5, low-temperature plasma is generated on the surface side of the catalyst layer 4.

When the low-temperature plasma heats the reaction gas or when the reaction gas is turned into plasma,
The reaction gas is excited. At the same time, the reaction gas is
And a product selected for the solid catalyst is produced. The generated substance (gas) is released from below the chamber 1.

According to such a gas production method, a substance requiring a high temperature and a high pressure can be produced at a normal pressure from normal temperature to about 200 ° C. at a normal pressure. The gas production apparatus does not require a heater and does not need to have a pressure-resistant structure. As a result,
Gas production equipment can be small. It should be noted that the pressure may be increased or reduced depending on the balance between the pre-process and the post-process.

The solid catalyst forming the catalyst layer 3 can be selected according to the reactants and the products. For example, when a mixed gas of hydrocarbon and water vapor is used as a reaction gas and a synthesis gas that is a mixed gas of carbon monoxide and hydrogen is used as a product, the solid catalyst is metallic nickel supported on alumina.

When a mixed gas of carbon monoxide and water vapor is used as a reaction gas and hydrogen is used as a product, the solid catalyst is metallic iron or metallic chromium.

When a mixed gas of a hydrocarbon and a nitrogen mixed gas is used as a reaction gas and ammonia is used as a product, the solid catalyst is metallic iron, alumina, or potassium oxide.

When a synthesis gas, which is a mixed gas of carbon monoxide and hydrogen, is used as a reaction gas and methane is used as a product, the solid catalyst is rhodium metal, nickel metal, thorium oxide, or magnesium oxide.

When the synthesis gas is used as the reaction gas and the paraffin / olefin is used as the product, the solid catalyst may be metallic iron,
Metal cobalt, nickel nickel, thorium oxide, magnesium oxide, alumina, or potassium oxide.

When the synthesis gas is used as the reaction gas and methanol is used as the product, the solid catalyst is zinc oxide, chromium oxide, metallic copper, or alumina.

When the synthesis gas is the reaction gas and ethanol is the product, the solid catalyst is rhodium metal, metal iron or silica.

When the synthesis gas is used as the reaction gas and the higher alcohol is used as the product, the solid catalyst is zinc oxide, chromium oxide, copper metal, or an alkali metal.

When the synthesis gas is the reaction gas and ethylene glycol is the product, the solid catalyst is a metal rhodium, metal potassium or cerium salt.

In another embodiment of the gas producing apparatus according to the present invention, a granular solid catalyst is provided. In the gas producing apparatus 20, as shown in FIG. 2, a chamber 21 forms a reaction gas flow path 22. The flow path 22 is parallel to the vertical direction, and the reaction gas flows vertically upward. An electrode 23 is formed on the inner wall of the chamber 21 and is grounded.

The channel 22 inside the chamber 21 is filled with a granular catalyst 24. Such a catalyst 24
Is preferred in that the contact area with the reaction gas is large. The catalyst 24 can flow, and flows when a reaction gas is blown into the flow path 22.

The gas producing apparatus 20 has an electrode 25. The electrode 25 has a rod shape and is disposed in the center of the flow channel 22 so as to extend in the vertical direction. The electrode 25 is the electrode 23
And is electrically insulated and fixed. Chamber 21
The upper and lower ends are open, the reaction gas flows in from the lower end of the chamber 21, and the product is released from the upper end of the chamber 21.

The gas producing apparatus 20 has a catalyst regeneration tower 30 and catalyst flow paths 31 and 32. Catalyst regeneration tower 30
Is regenerated by removing by-products attached to the catalyst 24. The flow path 31 is connected to the downstream side of the chamber 21, connected to the catalyst regeneration tower 30, and transports the catalyst 24 in the flow path 22 to the catalyst regeneration tower 30. The flow path 32 is connected to the catalyst regeneration tower 30 and is connected to the upstream side of the chamber 21, and transports the regenerated catalyst 24 into the chamber 21.

The gas producing apparatus 20 further includes a high-voltage power supply 1
1 is provided. The high-voltage power supply 11 includes an electrode 23 and an electrode 2
5, a high voltage is applied to generate low-temperature plasma.

The embodiment of the gas producing method according to the present invention includes flowing a reaction gas at room temperature and pressure from the lower end of the chamber 21 and applying a high voltage to the electrodes 23 and 25. First, a reaction gas is passed from the lower end of the chamber 21 to the flow path 22. After that, the high voltage power supply 11
When a high voltage is applied to 25, low-temperature plasma is generated in the gap of the catalyst 24.

When the low-temperature plasma heats the reaction gas, or when the reaction gas turns into plasma,
The reaction gas is excited. At the same time, the reaction gas
To produce the selected product on the catalyst 24. The generated substance (gas) is released from above the chamber 22.

The catalyst 24 flows and is transported to the catalyst regeneration tower 30 by the flow of the reactant gas and the release of the product. Catalyst 24 regenerated by catalyst regeneration tower 30
Is returned to the chamber 21 and again acts as a catalyst.
When excited by the low-temperature plasma, a large amount of by-products are generated and adhere to the surface of the catalyst 24. When the amount of the catalyst 24 having the by-product adhered to the surface increases, the catalyst selectivity of the produced substance deteriorates. The catalyst regeneration tower 30 extends the life of the catalyst selectivity of the product and improves the yield of the product.

The solid catalyst forming the catalyst 23 depends on the reactants and products in the same manner as in the previous embodiment.
You can choose.

In the embodiment of the fuel cell according to the present invention, the gas producing apparatus according to the present invention is provided in the fuel cell main body. The gas producing apparatus is configured in the same manner as in the previous embodiment. The reaction gas is a mixed gas of hydrocarbon and water vapor, and the product is hydrogen. The solid catalyst is metallic nickel supported on alumina. Note that a mixed gas of carbon monoxide and water vapor can be used as a reaction gas. In this case, the solid catalyst is metallic iron or metallic chromium.

The fuel cell body generates electric power from hydrogen and oxygen mixed gas. The oxygen mixture gas is preferably ambient air. Such a fuel cell body is known.

The fuel cell according to the present invention does not need to supply hydrogen directly, and is easy to handle.

[0077]

According to the gas producing apparatus and the gas producing method of the present invention, when producing a useful gas, it is possible to reduce the energy input for promoting the reaction.

[Brief description of the drawings]

FIG. 1 is a sectional view showing an embodiment of a gas producing apparatus according to the present invention.

FIG. 2 is a sectional view showing another embodiment of the gas producing apparatus according to the present invention.

FIG. 3 is a block diagram showing an embodiment of a known synthesis gas production apparatus.

FIG. 4 is a block diagram showing an embodiment of a known hydrogen gas producing apparatus.

FIG. 5 is a block diagram showing an embodiment of a known ammonia producing apparatus.

FIG. 6 is a block diagram showing an embodiment of a known useful gas producing apparatus.

FIG. 7 is a cross-sectional view showing an embodiment of a known low-temperature plasma reaction reactor.

[Explanation of symbols]

 1,21 ... chamber 2,22 ... flow path 3,23 ... electrode 4 ... catalyst layer 5,25 ... electrode 6 ... inlet 24 ... catalyst

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) H01M 8/06 C10L 3/00 A

Claims (25)

[Claims] 1. A reaction tower forming a flow path of a gaseous reactant, a catalyst disposed in the flow path, a first electrode, and a second electrode, wherein the first electrode, the second electrode, A low-temperature plasma generated in the vicinity of the surface of the catalyst based on a voltage applied during the step of exciting the gaseous reactant to generate a product. 2. The method according to claim 1, wherein the first electrode is disposed on an inner wall of the reaction tower, the second electrode is disposed in the flow path, and the catalyst covers the second electrode. Gas production equipment. 3. The gas production apparatus according to claim 1, wherein the catalyst is granular and is filled in the flow path. 4. The gas producing apparatus according to claim 3, wherein the catalyst is capable of flowing. 5. The method according to claim 1, wherein the gaseous reactant is a synthesis gas, the product is methane, and the catalyst is rhodium, nickel, thorium oxide, or oxidized gas. Gas production equipment that is magnesium. 6. The method according to claim 1, wherein the gaseous reactant is a synthesis gas, the product is a paraffin or an olefin, and the catalyst is metallic iron, metallic cobalt, metallic nickel. Gas producing device which is thorium oxide, magnesium oxide, alumina or potassium oxide. 7. The method according to claim 1, wherein said gaseous reactant is a synthesis gas, said product is methanol, and said catalyst is zinc oxide, chromium oxide, zinc oxide, metal Gas production equipment that is copper or alumina. 8. The method according to claim 1, wherein the gaseous reactant is a synthesis gas, the product is ethanol, and the catalyst is metal rhodium, metal iron or silica. A gas production device. 9. The method according to claim 1, wherein the gaseous reactant is a synthesis gas, the product is a higher alcohol, and the catalyst is zinc oxide, chromium oxide, zinc oxide, Gas production equipment made of copper metal or alkali metal. 10. The method according to claim 1, wherein the gaseous reactant is a synthesis gas, the product is ethylene glycol, and the catalyst is metal rhodium, metal potassium, or cerium. Gas production equipment. 11. The method according to claim 1, wherein the gaseous reactant is a hydrocarbon and water vapor, the product is a synthesis gas, and the catalyst is supported on alumina. Gas production equipment that is metallic nickel. 12. The method according to claim 1, wherein the gaseous reactant is carbon monoxide and water vapor, the product is hydrogen, and the catalyst is metallic iron or metallic nickel. Gas production equipment. 13. The method according to claim 1, wherein the gaseous reactant is a mixture of hydrocarbon and nitrogen, the product is ammonia, and the catalyst is metallic iron or alumina. Or a gas production device that is potassium oxide. 14. A reaction tower for forming a flow path of a gaseous reactant for mixing a hydrocarbon and steam, a catalyst disposed in the flow path and being metal iron, metal nickel, metal chromium, or alumina; An electrode, a second electrode that is a counter electrode of the first electrode, and a fuel cell main body, wherein the first electrode generates low-temperature plasma on the surface of the catalyst together with the second electrode; A fuel cell that excites the gaseous reactant to generate hydrogen, and the fuel cell body generates electric power from a chemical reaction between the hydrogen and an oxygen mixed gas. 15. A method for producing a gas, comprising: exciting a gaseous reactant with low-temperature plasma; causing a catalyst to act on the gaseous reactant; and producing a product from the gaseous reactant. 16. The gas production method according to claim 15, further comprising: supplying thermal energy to the gaseous reactant by the low-temperature plasma. 17. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is methane, the catalyst is rhodium,
A gas production method that is nickel, thorium oxide, or magnesium oxide. 18. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is a paraffin olefin, and the catalyst is metallic iron, metallic cobalt, metallic nickel. Gas production method, which is thorium oxide, magnesium oxide, alumina or potassium oxide. 19. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is methanol, and the catalyst is zinc oxide, chromium oxide, metallic copper, or , A gas production method that is alumina. 20. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is ethanol, and the catalyst is rhodium, metallic iron, or silica. Gas production method. 21. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is a higher alcohol, and the catalyst is zinc oxide, chromium oxide, metallic copper, Alternatively, a gas production method that is an alkali metal. 22. The method according to claim 15, wherein the gaseous reactant is a synthesis gas, the product is ethylene glycol, and the catalyst is metal rhodium, metal potassium, or cerium. Gas production method. 23. The method according to claim 15, wherein the gaseous reactant is a hydrocarbon and water vapor, the product is a synthesis gas, and the catalyst is supported on alumina. Gas production method that is metallic nickel. 24. The method according to claim 15, wherein the gaseous reactant is carbon monoxide and water vapor, the product is hydrogen, and the catalyst is metallic iron or metallic nickel. Gas production method. 25. The method according to claim 15, wherein the gaseous reactant is a hydrocarbon and a nitrogen mixed gas, the product is ammonia, and the catalyst is metallic iron, alumina. Or a gas production method that is potassium oxide.