JP2006162243A - Gaseous hydrogen removing device - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a gaseous hydrogen removing device capable of reducing a load relevant to maintenance for gaseous hydrogen removing capacity recovery. <P>SOLUTION: The gaseous hydrogen removing device is composed so as to oxidize and remove gaseous hydrogen generated in a gaseous hydrogen removal target device by an oxidization part Ox including metallic oxide. The oxidization part Ox is composed of a porous sintered body 51 of the metallic oxide. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a hydrogen gas removal apparatus configured to oxidize and remove hydrogen gas generated in an apparatus of a hydrogen gas removal target apparatus in an oxidation unit containing a metal oxide.

Such a hydrogen gas removing device removes the hydrogen gas by oxidizing the hydrogen gas generated in the device of the hydrogen gas removing target device such as an absorption refrigeration machine in an oxidizing portion so that the hydrogen gas can be condensed. It is composed.
That is, in an absorption refrigerator as an example of an apparatus for removing hydrogen gas, as a device constituent material that constitutes a regenerator, a condenser, an absorber and an evaporator, and pipes connecting them, generally iron or stainless steel The combination of water and lithium bromide, or the combination of ammonia and water, etc. is used as the combination of refrigerant and absorbent. Reaction with the solution generates hydrogen gas. This hydrogen gas does not condense in the absorption refrigerator, but stays in the vapor phase of the evaporator or absorber, and the internal pressure of the evaporator or absorber that requires a low pressure gradually increases. As a result, the capacity of the absorption refrigerator is reduced.
Therefore, a hydrogen gas removing device is provided to remove the hydrogen gas in the absorption chiller so as to suppress a reduction in the capacity of the absorption chiller.

In such a hydrogen gas removal apparatus, conventionally, the oxidation part has been composed of porous spherical alumina carrying a metal oxide.
By the way, porous spherical alumina is immersed in an aqueous solution containing copper ions, impregnated with porous spherical alumina with copper ions, and oxidized at a high temperature, so that copper oxide as a metal oxide is added to porous spherical alumina. (See, for example, Patent Document 1).

JP 59-32942 A

  By the way, such a hydrogen gas removal apparatus oxidizes the hydrogen gas generated in the apparatus of the hydrogen gas removal target apparatus with the metal oxide of the oxidation part, in other words, the apparatus of the hydrogen gas removal target apparatus. By reducing the metal oxide in the oxidation part with hydrogen gas generated inside, water vapor is generated to remove the hydrogen gas. Accordingly, when the reduction of the metal oxide in the oxidized portion by hydrogen gas proceeds and the content of the metal oxide in the oxidized portion decreases, the hydrogen gas removal capability decreases, so the content of the metal oxide in the oxidized portion is reduced. Maintenance is required to restore the hydrogen gas removal capacity to a high level. In the maintenance for recovering the hydrogen gas removal capability, for example, the oxidized portion where the reduction of the metal oxide has progressed is removed from the hydrogen gas removal target device and heated in an oxygen-containing atmosphere to oxidize the metal and thereby oxidize the metal. By increasing the content of the product, the oxidized portion with the increased content of the metal oxide is loaded into the apparatus for removing hydrogen gas.

  Then, the larger the ratio of the volume of the metal oxide to the volume of the entire oxidized portion when it is assumed that the inside is filled (hereinafter sometimes referred to as the volume efficiency of the metal oxide), the larger the portion in the oxidized portion. It is possible to lengthen the time until the metal oxide content decreases to such an extent that the hydrogen gas removal capacity is affected, and the maintenance frequency for recovering the hydrogen gas removal capacity can be reduced. Become.

However, in the conventional hydrogen gas removal apparatus, since the oxidation part is composed of porous spherical alumina supporting a metal oxide, the volume of the metal oxide is equivalent to the presence of porous spherical alumina in the oxidation part. It is difficult to increase efficiency.
Therefore, conventionally, since it is difficult to increase the volumetric efficiency of the metal oxide in the oxidation portion, the time until the content of the metal oxide in the oxidation portion is reduced to such an extent that the hydrogen gas removal ability is affected is short. It is necessary to increase the frequency of maintenance for recovering the gas removal capacity, and the burden on the maintenance has been large.

  This invention is made | formed in view of this situation, The objective is to provide the hydrogen gas removal apparatus which can reduce the burden concerning the maintenance for hydrogen gas removal capability recovery.

The hydrogen gas removal device of the present invention is configured to oxidize and remove the hydrogen gas generated in the device of the hydrogen gas removal target device in an oxidation part containing a metal oxide,
The first characteristic configuration is characterized in that the oxidation part is formed of a porous sintered body of metal oxide.

That is, the oxidation part is composed of a metal oxide porous sintered body (hereinafter sometimes simply referred to as a porous sintered body), and the porous sintered body is made only of metal oxide. Or the volume efficiency of the metal oxide in the oxidation part can be increased because the amount of the components other than the metal oxide can be reduced as much as possible. It becomes possible.
And since it becomes possible to increase the volumetric efficiency of the metal oxide in the oxidation part, the time until the content of the metal oxide in the oxidation part is reduced to such an extent that the hydrogen gas removal ability is affected is lengthened. Therefore, the frequency of maintenance for recovering the hydrogen gas removal capability can be reduced.
Therefore, it has become possible to provide a hydrogen gas removing device that can reduce the burden on maintenance for recovering the hydrogen gas removing ability.

In addition to the first feature configuration, the second feature configuration is
In the porous sintered body, a mixture of a metal oxide powder and a binder having a boiling point lower than that of the metal oxide is heated to a temperature higher than the boiling point of the binder to sinter the metal oxide powder into a porous form. It is characterized by being formed by bonding.

That is, when a mixture of a metal oxide powder and a binder having a boiling point lower than that of the metal oxide is heated to a temperature higher than the boiling point of the binder, the binder evaporates and escapes from the mixture, and the removed portion becomes pores. In this state, the metal oxide powder is sintered, and the metal oxide powder is sintered in a porous state, so that a porous sintered body is formed.
By the way, a mixture of metal powder and binder is heated and sintered while oxidizing the metal during the heating process to form a porous sintered body, or a mixture of metal powder and binder is used. It may be possible to sinter metal powder by heating and oxidize the metal after the sintering to form a porous sintered body. In these cases, the metal powder is oxidized in the porous sintered body. There is a possibility that a metal portion that is not left will remain, which is somewhat disadvantageous in increasing the volumetric efficiency of the metal oxide.
On the other hand, it is preferable to increase the volume efficiency of the metal oxide by heating the mixture of the metal oxide powder itself and the binder to form a porous sintered body.
Accordingly, it is possible to provide a suitable means for further increasing the volumetric efficiency of the metal oxide and further reducing the burden on maintenance for recovering the hydrogen gas removal capability.

In addition to the first or second feature configuration, the third feature configuration is
The metal oxide is cupric oxide (CuO), and the density of the porous sintered body of cupric oxide is 4.0 g / cm ³ or more.

That is, the inventors of the present invention have eagerly studied to further reduce the burden on maintenance for recovering the hydrogen gas removal capability, and in the one having the first or second characteristic configuration described above, as a metal oxide When cupric oxide is used and the density of the porous sintered body of cupric oxide is set to 4.0 g / cm ³ or more, the burden on maintenance for recovering the hydrogen gas removal capability is further reduced. It was found that this is preferable.

In other words, since cupric oxide has a strong oxidizing power, the use of cupric oxide as a metal oxide can further improve the hydrogen gas removal capability, and further, the porous sintering of the cupric oxide is porous. By setting the density of the body to 4.0 g / cm ³ or more and increasing the volumetric efficiency of the metal oxide, hydrogen gas is infiltrated into the porous sintered body of cupric oxide, and the hydrogen gas In reducing the metal oxide to remove the hydrogen gas, it was found that the hydrogen gas removal ability can be increased.

By the way, there is a case where the porous sintered body of cupric oxide is heated from the outside to a temperature suitable for the reduction reaction to remove hydrogen gas. In such a case, the density of the porous sintered body is reduced. If it is increased, the heat conduction of the porous sintered body increases, the temperature distribution can be reduced over the entire porous sintered body, and the temperature suitable for the reduction reaction is maintained over the entire porous sintered body. Therefore, the hydrogen gas removal capability can be increased from this point.
Therefore, by using cupric oxide as the metal oxide and setting the density of the porous sintered body of cupric oxide to 4.0 g / cm ³ or more, the hydrogen gas removal capability can be improved. As a result, the burden on maintenance for recovering the hydrogen gas removal capability can be further reduced.

In addition to the first or second feature configuration, the fourth feature configuration is
The metal oxide is nickel monoxide (NiO), and the density of the porous sintered body of nickel monoxide is in the range of 5.0 to 6.5 g / cm ³ .

That is, the inventors of the present invention have eagerly studied to further reduce the burden on maintenance for recovering the hydrogen gas removal capability, and in the one having the first or second characteristic configuration described above, as a metal oxide When nickel monoxide is used and the density of the porous sintered body of nickel monoxide is set in the range of 5.0 to 6.5 g / cm ³ , the burden on maintenance for recovering the hydrogen gas removal capability is reduced. At the same time, the present inventors have found that it is preferable to improve the hydrogen gas removal capability.

That is, since nickel monoxide has a strong oxidizing power, the ability to remove hydrogen gas can be further improved by using nickel monoxide as the metal oxide.
And if the density of the porous sintered body is set to be smaller than 5.0 g / cm ³ , the volume efficiency of the metal oxide becomes small, so the frequency of maintenance for recovering the hydrogen gas removal capability tends to increase. If the density of the porous sintered body is set to be larger than 6.5 g / cm ³ , the volume efficiency of the metal oxide increases, and the frequency of maintenance for recovering the hydrogen gas removal capability can be reduced. However, since the pores of the porous sintered body are too fine and hydrogen gas hardly penetrates into the porous sintered body, the hydrogen gas removing ability tends to be low.
Then, by setting the density of the porous sintered body of nickel monoxide in the range of 5.0 to 6.5 g / cm ³ , the hydrogen gas is porous sintered while increasing the volume efficiency of the metal oxide. It becomes possible to make it easy to penetrate into the body, and the hydrogen gas removing ability can be increased.
Therefore, by using nickel monoxide as the metal oxide and setting the density of the porous sintered body of nickel monoxide in the range of 5.0 to 6.5 g / cm ³ , the hydrogen gas removal capability is improved. As a result, the burden on maintenance for recovering the hydrogen gas removal capability can be further reduced.

In addition to the first or second feature configuration, the fifth feature configuration includes:
The metal oxide is cobalt monoxide (CoO), and the density of the porous sintered body of cobalt monoxide is in the range of 4.0 to 6.2 g / cm ³ .

That is, the inventors of the present invention have eagerly studied to further reduce the burden on maintenance for recovering the hydrogen gas removal capability, and in the one having the first or second characteristic configuration described above, as a metal oxide When cobalt monoxide is used and the density of the porous sintered body of cobalt monoxide is set in the range of 4.0 to 6.2 g / cm ³ , the burden on maintenance for recovering the hydrogen gas removal capability is reduced. At the same time, the present inventors have found that it is preferable to improve the hydrogen gas removal capability.

That is, since cobalt monoxide has a strong oxidizing power, the ability to remove hydrogen gas can be further improved by using cobalt monoxide as the metal oxide.
Then, by setting the density of the porous sintered body of cobalt monoxide in the range of 4.0 to 6.2 g / cm ³ , the metal oxide is the same as described for the fourth characteristic configuration. While increasing the volumetric efficiency, it is possible to make hydrogen gas easily permeate into the porous sintered body, thereby increasing the hydrogen gas removal capability.
Therefore, by using cobalt monoxide as the metal oxide and setting the density of the porous sintered body of cobalt monoxide in the range of 4.0 to 6.2 g / cm ³ , the hydrogen gas removal capability is improved. As a result, the burden on maintenance for recovering the hydrogen gas removal capability can be further reduced.

In addition to the first or second feature configuration, the sixth feature configuration is
An average pore radius of the porous sintered body is in a range of 300 to 3000 nm.

  That is, the inventors of the present invention have intensively studied to further reduce the burden related to maintenance for recovering the hydrogen gas removal capability, and in the one having the first or second characteristic configuration described above, porous sintering It was found that setting the average pore radius of the body in the range of 300 to 3000 nm is preferable in reducing the burden on maintenance for recovering the hydrogen gas removal capability and improving the hydrogen gas removal capability. .

  In other words, if the average pore radius of the porous sintered body is set to be larger than 3000 nm, the volume efficiency of the metal oxide is reduced, so that the frequency of maintenance for recovering the hydrogen gas removal capability tends to increase, If the average pore radius of the sintered body is set to be smaller than 300 nm, the volume efficiency of the metal oxide increases, and the frequency of maintenance for recovering the hydrogen gas removal capability can be reduced. Since the pores of the sintered body are too fine and it is difficult for hydrogen gas to penetrate into the porous sintered body, the hydrogen gas removal capability tends to be low.

When the average pore radius of the porous sintered body is set in the range of 300 to 3000 nm, the volume efficiency of the metal oxide is increased, and the hydrogen gas can easily penetrate into the porous sintered body. This makes it possible to increase the hydrogen gas removal capability.
Therefore, by setting the average pore radius of the porous sintered body in the range of 300 to 3000 nm, the hydrogen gas removal capability can be improved, so that the burden on maintenance for recovering the hydrogen gas removal capability is further increased. It can be further reduced.

In addition to any one of the first to sixth characteristic configurations, the seventh characteristic configuration is that the particle size of most of the raw material powder of the metal oxide forming the porous sintered body is 0.1 to 10 μm. It is characterized by a range.

  That is, the inventors of the present invention have intensively studied to reduce the burden on maintenance for recovering the hydrogen gas removal capability while reducing the cost of the apparatus, and any one of the first to sixth feature configurations described above. If the particle size of most of the metal oxide raw material powder forming the porous sintered body is set in the range of 0.1 to 10 μm, the hydrogen gas removal ability is recovered while reducing the cost of the apparatus. We found that it is preferable in reducing the burden on maintenance for

That is, among the metal oxide raw material powders forming the porous sintered body, the larger the particle size is smaller than 0.1 μm, the higher the density of the porous sintered body can be. As the price of the material increases, the apparatus becomes more expensive, and among the metal oxide raw material powders forming the porous sintered body, the larger the particle size is larger than 10 μm, the more the porous sintered body becomes As the density decreases, the frequency of maintenance for recovering the hydrogen gas removal capability tends to increase.
When the particle size of most of the raw material powder of the metal oxide forming the porous sintered body is set in the range of 0.1 to 10 μm, it is possible to recover the hydrogen gas removal capability while reducing the cost of the apparatus. They found that the burden on maintenance could be reduced.
Therefore, by setting the particle size of most of the metal oxide raw material powder forming the porous sintered body in the range of 0.1 to 10 μm, the hydrogen gas removal ability can be recovered while reducing the cost of the apparatus. The burden on maintenance can be reduced.

In addition to any of the first to seventh features described above, the eighth characteristic configuration is
The hydrogen gas removal target device is an absorption refrigerator.

That is, the hydrogen gas generated in the absorption refrigerator as described above is oxidized by the metal oxide in the oxidation portion to become water vapor in a condensable state, and the hydrogen gas is removed.
And, it is possible to increase the volume efficiency of the metal oxide and reduce the frequency of maintenance for recovering the hydrogen gas removal capability by configuring the oxidized portion with a porous sintered body of the metal oxide. It becomes.
Therefore, it has become possible to provide a hydrogen gas removal device for an absorption refrigeration machine that can reduce the burden on maintenance for recovering the hydrogen gas removal capability.

Hereinafter, a first embodiment in the case where the present invention is applied to a hydrogen gas removing device for an absorption refrigerator will be described with reference to the drawings.
First, a double-effect absorption refrigerator equipped with a hydrogen gas removing device E will be described with reference to FIG.
This absorption refrigerator uses water as a refrigerant and uses lithium bromide as an absorbent. The evaporator 1 evaporates the refrigerant liquid, and the refrigerant vapor generated in the evaporator 1 is an aqueous solution of the absorbent. Absorber 2 to be absorbed by the absorbing liquid, and high-temperature regeneration that generates the refrigerant vapor from the diluted liquid by heating the low-concentration absorbing liquid (hereinafter sometimes referred to as a diluted liquid) that has absorbed the refrigerant vapor by the absorber 2 Refrigerant vapor is heated by the refrigerant vapor generated in the high-temperature regenerator 3, and the absorbing liquid having a medium concentration due to the generation of refrigerant vapor by the high-temperature regenerator 3 (hereinafter, sometimes referred to as intermediate liquid). A low-temperature regenerator 4 that further generates the refrigerant, a high-temperature regenerator 3, a condenser 5 that condenses the refrigerant vapor generated in the low-temperature regenerator 4, and a hydrogen gas removal device E that removes hydrogen gas generated in the absorption refrigerator Etc., and the absorber 2 includes Temperature regenerator 4 absorption liquid becomes highly concentrated in the occurrence of refrigerant vapor by being adapted to provide (hereinafter, sometimes referred to as concentrated liquid).

Hereinafter, each part of the absorption chiller will be described.
The evaporator 1 and the absorber 2 are integrally configured using a container 6. In other words, the inside of the container 6 is divided in the lateral direction by the partition body 7 in a state of allowing air to pass therethrough, and the refrigerant spraying tool 8 for spraying the refrigerant liquid on one side of the container 6 and the refrigerant liquid by the refrigerant spraying tool 8. Is disposed, and an evaporator liquid reservoir 10 that stores the refrigerant liquid sprayed from the refrigerant sprayer 8 is provided to constitute the evaporator 1, and the other side in the container 6. In addition, an absorbent dispersion tool 11 for spraying the concentrated liquid and an absorber coil 12 for spraying the concentrated liquid in the absorbent dispersion tool 11 are disposed, and the refrigerant vapor generated in the evaporator 1 is absorbed. The absorber 2 is configured by forming an absorber liquid reservoir 13 for storing the diluted liquid at the bottom of the container 6.

The evaporator liquid reservoir 10 is supplied with a refrigerant liquid from a condenser liquid reservoir 14 of the condenser 5 to be described later through a refrigerant liquid supply passage 15, and the refrigerant liquid in the evaporator liquid reservoir 10 is supplied to the refrigerant by a refrigerant pump 16. The refrigerant is sprayed to the refrigerant spreader 8 through the liquid circulation path 17.
A concentrated liquid is supplied to the absorbing liquid spreader 11 from a low temperature regenerator liquid reservoir 18 of the low temperature regenerator 4 described later through a concentrated liquid path 19.

  The evaporator coil 9 is caused to pass cold water through a cold water passage 20 for taking out cold water, and the absorber coil 12 is caused to pass cooling water through a cooling water passage 21. The cooling water passage 21 is piped so that the cooling water flows in the order of the absorber coil 12 and the condenser coil 22 of the condenser 5 described later.

The dilute liquid in the absorber liquid reservoir 13 is supplied to the high temperature regenerator 3 through the dilute liquid path 24 by the absorption liquid pump 23, and the high temperature regenerator 3 heats the absorption liquid by the combustion of the gas burner 25 to generate refrigerant vapor. generate.
Reference numeral 26 in the figure denotes a separator that separates the absorbing liquid from the refrigerant vapor generated in the high-temperature regenerator 3, and the refrigerant vapor separated from the absorbing liquid in the separator 26 passes through the refrigerant vapor passage 27 to be described later. After passing through the low-temperature regenerator coil 28 of the regenerator 4, the regenerator 4 is supplied into the condenser 5.
The separator 26 is internally provided with a separator 26a that separates the liquid absorbent in the form of droplets accompanying the refrigerant vapor.

  Reference numeral 29 in the figure denotes a hot water heater for taking out hot water. The hot water heater 29 heats the refrigerant vapor taken out from the high-temperature regenerator 3 through the refrigerant vapor take-out passage 30 and hot water flowing through the hot water passage 31. The hot water is heated by the sensible heat and the latent heat of condensation of the refrigerant vapor, and the hot water is taken out through the hot water channel 31.

  The low-temperature regenerator 4 and the condenser 5 are configured integrally using a container 32. That is, the low-temperature regenerator in which the inside of the container 32 is divided in the horizontal direction by the partition 33 in a state where it can be vented and the medium liquid is supplied from the high-temperature regenerator 3 to the one side in the container 32 through the medium-liquid passage 34. The liquid reservoir 18 and the low temperature regenerator coil 28 to which the refrigerant vapor is supplied from the high temperature regenerator 3 through the refrigerant vapor path 27 are provided to constitute the low temperature regenerator 4, and on the other side in the container 32. The condenser 5 is configured by providing the condenser liquid reservoir 14 and the condenser coil 22 to which cooling water is supplied through the cooling water passage 21.

Then, in the low temperature regenerator 4, the absorption liquid in the low temperature regenerator liquid reservoir 18 is heated by the refrigerant vapor flowing through the low temperature regenerator coil 28 to generate refrigerant vapor, and the absorption liquid is concentrated as such. The concentrated concentrate is supplied to the absorbent dispersion tool 11 of the absorber 2 through the concentrated liquid path 19.
In the condenser 5, the cooling of the refrigerant vapor supplied from the high temperature regenerator 3 through the refrigerant vapor path 27 and the refrigerant vapor supplied from the low temperature regenerator 4 through the partition 33 through the condenser coil 22. After cooling with water and condensing, the refrigerant liquid is stored in the condenser liquid reservoir 14, and the refrigerant liquid in the condenser liquid reservoir 14 is passed through the refrigerant liquid supply path 15 to the evaporator liquid reservoir 10 of the evaporator 1. To supply.

  Further, the high temperature heat exchanger 35 for heating the dilute liquid flowing through the dilute liquid path 24 by the medium liquid flowing through the intermediate liquid path 34 and the dilute liquid path 24 by the concentrated liquid flowing through the concentrated liquid path 19 are used. A low-temperature heat exchanger 36 for heating the dilute liquid flowing therethrough is provided.

This absorption refrigerator is configured to be switchable between a cooling operation in which cold water is taken out through the cold water passage 20 and a heating operation in which hot water is taken out through the hot water passage 31. A dilute liquid path open / close valve 37 is provided, a middle liquid path open / close valve 38 is provided in the intermediate liquid path 34, a refrigerant vapor path open / close valve 39 is provided between the separator 26 and the low temperature regenerator coil 28, And it is located between each of the low temperature regenerator coil 28 and the condenser 5.
When the cooling operation is executed, the absorption liquid pump 23 and the refrigerant pump 16 are operated, and the dilute liquid path open / close valve 37, the middle liquid path open / close valve 38, and the two refrigerant vapor path open / close valves 39 are all opened. When the heating operation is performed, the absorption liquid pump 23 and the refrigerant pump 16 are stopped, and the dilute liquid path open / close valve 37, the middle liquid path open / close valve 38, and the two refrigerant vapor path open / close valves 39 are all turned on. It will be closed.

That is, in the cooling operation, the refrigerant vapor generated in the high temperature regenerator 3 and the low temperature regenerator 4 is supplied to the condenser 5, and the refrigerant vapor is condensed by the action of the condenser coil 22 to condense the refrigerant liquid. The refrigerant is stored in the liquid reservoir 14 and the refrigerant liquid in the condenser liquid reservoir 14 is supplied to the evaporator liquid reservoir 10. And the refrigerant | coolant liquid of the evaporator liquid storage part 10 is spread | dispersed in the evaporator 1 from the refrigerant | coolant spraying tool 8 with the refrigerant | coolant pump 16, the sprayed refrigerant | coolant liquid is evaporated by the effect | action of the evaporator coil 9, and the evaporation By taking the heat of vaporization, the cold water flowing through the evaporator coil 9 is cooled, and the cold water is taken out through the cold water passage 20.
On the other hand, the absorbing liquid from the low temperature regenerator 4 is sprayed from the absorbing liquid sprayer 11 into the absorber 2, and the sprayed absorbing liquid absorbs the refrigerant vapor generated in the evaporator 1 and absorbs the refrigerant vapor. The absorbing liquid having a reduced concentration is passed through the high-temperature regenerator 3 and the low-temperature regenerator 4 in order, and refrigerant vapor is generated from the absorbing liquid in each of the high-temperature regenerator 3 and the low-temperature regenerator 4 to absorb the absorbing liquid. And the concentrated absorbent is sprayed from the absorbent sprayer 11 into the absorber 2 as described above.
Further, the heat generated by the concentrated liquid absorbing the refrigerant vapor in the absorber 2 is given to the cooling water flowing through the absorber coil 12, and the condensation generated by the refrigerant vapor condensing in the condenser 5. Heat is given to the cooling water flowing through the condenser coil 22, and the absorption heat and condensation heat are taken out through the cooling water.

  Furthermore, in this absorption refrigerator, the suction part 41 acting on the low-pressure part (for example, the evaporator 1 or the absorber 2) in the circulation system of the absorption liquid and the refrigerant, and the suction part 41 sucked in the suction part 41 By providing a storage tank 42 for storing hydrogen gas and providing the hydrogen gas removal device E in the storage tank 42, the hydrogen gas generated in the absorption chiller is stored in the storage tank 42 by the hydrogen gas removal device E. By removing the pressure, the pressure inside the machine due to the generation of hydrogen gas (especially, the rise in the pressure inside the evaporator 1 or the absorber 2 where low pressure is required) is prevented, and the capacity reduction of the absorption refrigerator is prevented. It is.

  The suction unit 41 uses the ejector 44 to suck a part of the diluted liquid sent out by the absorption liquid pump 23 as a driving fluid into the absorber configuration space in the container 6, that is, the absorption path through the suction path 46 in the absorber 2. A part of the dilute liquid sent out by the absorption liquid pump 23 is guided to the ejector 44 by the dilute liquid branching path 45 as a driving fluid, and the absorber 2 passes through the suction path 46 by the high-speed flow of the dilute liquid. The gas inside the absorber 2 (including refrigerant vapor and hydrogen gas) is sucked by suction. Incidentally, since the evaporator 1 and the absorber 2 are configured to communicate with each other in the container 6 as described above, the internal gas (including refrigerant vapor and hydrogen gas) of the evaporator 1 is also sucked into the suction path. Aspirate through 46.

The storage tank 42 is arranged in a state of being connected to the ejection port of the ejector 44 through a U-shaped ejection path 47, and the mixed tank of the rare liquid ejected from the ejector 44 and the gas in the container is stored through the ejection path 47. In the storage tank 42, the dilute liquid and the non-condensable hydrogen gas are stored in a gas-liquid separation state.
The ejection path 47 is provided with a check valve 48 that prevents the backflow of fluid from the storage tank 42 to the ejector 44.
The storage tank 42 and the absorber 2 are connected by a U-shaped dilute liquid return path 49, and the dilute liquid separated from the hydrogen gas in the storage tank 42 is absorbed through the dilute liquid return path 49. It is configured to return to the second absorber liquid reservoir 13.

Next, the hydrogen gas removing device E will be described based on FIG.
This hydrogen gas removing device E includes an oxidized portion Ox containing a metal oxide (in this embodiment, cupric oxide (CuO)), an electric heater 52 as a heating means for heating the oxidized portion Ox, and the oxidized portions. A device block 53 made of corrosion-resistant metal on which Ox and an electric heater 52 are mounted, and the hydrogen gas in the storage tank 42 is oxidized with metal oxide to be in a condensable state (water vapor). The hydrogen gas is removed.
Further, the oxidation part Ox is heated by the electric heater 52 to promote the oxidation reaction, thereby efficiently removing the hydrogen gas in the machine.

  The oxidized portion Ox is composed of a metal oxide porous sintered body 51.

Next, an attachment configuration for attaching the hydrogen gas removing device E to the storage tank 42 will be described.
An attachment wall 42b of the hydrogen gas removal device E is formed in the device wall 42a (in this embodiment, the upper wall) surrounding the gas phase portion of the storage tank 42 in the device wall forming the storage tank 42, and the porous firing is performed. By connecting and fixing the device block 53 equipped with the combined body 51 and the electric heater 52 to the instrument wall 42a while being inserted into the mounting port 42b from the outside of the storage tank 42, the hydrogen gas removing device E is attached to the storage tank 42. Install.

  Further, in this attachment, the device block 53 is connected and fixed to the instrument wall 42a by a connecting means that can be connected and disconnected by a bolt or the like while straddling the inside and the outside of the storage tank 42. The container wall 42a is sealed by a sealing means.

  That is, the hydrogen gas removing device E is detachably attached to the device wall 42a of the storage tank 42 in a state in which it forms a part of the device wall of the storage tank 42 (in other words, a lid for the attachment port 42b). This facilitates assembly of the hydrogen gas removing device E at the time of manufacture, maintenance of the hydrogen gas removing device E after that, and the like.

The apparatus block 53 is formed with an oxidation portion accommodation hole 53a that opens to the gas phase portion of the storage tank 42 and a heater insertion hole 53b that opens to the outside of the storage tank 42 when the device block 53 is attached to the vessel wall 42a. The porous sintered body 51 is accommodated in the oxidation portion collecting hole 53a and attached to the apparatus block 53, and the electric heater 52 is inserted into the heater insertion hole 53b so as to be fitted in the apparatus block 53.
That is, the hydrogen gas in the storage tank 42 is caused to flow into the oxidation portion accommodation hole 53a through the filter 54 so that the hydrogen gas reacts with the porous sintered body 51 under heating by the electric heater 52 in the oxidation portion accommodation hole 53a. In addition, the electric heater 52 can be removed from the apparatus block 53 without breaking the airtightness of the storage tank 42 during maintenance.

  Moreover, when the reduction of the metal oxide of the porous sintered body 51 proceeds with hydrogen gas, the metal oxide content decreases, and maintenance for recovering the hydrogen gas removal capability is required, the hydrogen gas removal The apparatus E is removed from the storage tank 42, and the porous sintered body 51 is taken out from the oxidation part accommodation hole 53a. And the taken-out porous sintered body 51 is heated in an oxidizing atmosphere to oxidize a metal (copper in this embodiment) to recover the hydrogen gas removing ability.

Further, the hydrogen gas removing device E is equipped with a heating temperature sensor 57 for detecting the temperature of the porous sintered body 51.
The controller 55 that controls the operation of the absorption chiller is configured to execute an oxidation unit temperature control that adjusts the output of the electric heater 52 so that the temperature detected by the heating temperature sensor 57 becomes a set temperature. It is. The set temperature is set in a range of 120 to 250 ° C. and stored in the controller 55.

A method for manufacturing the porous sintered body 51 will be described.
This porous sintered body 51 is made of a mixture of a powder of metal oxide (cupric oxide in this embodiment) and a binder (polyvinyl alcohol in this embodiment) having a boiling point lower than that of the metal oxide. The metal oxide powder is heated to a temperature higher than the boiling point, and the metal oxide powder is sintered into a porous shape.
The density of the cuprous oxide porous sintered body 51 is preferably set to 4.0 g / cm ³ or more.
However, since the specific gravity of the cupric oxide crystal is 6.4, the density of the porous sintered body 51 of cupric oxide is smaller than 6.4 g / cm ³ .

More specifically, a mixture of a metal oxide and a binder is pressure-molded into a predetermined shape (cylindrical shape, spherical shape, cubic shape, rectangular parallelepiped shape, etc.), and the pressure-formed metal oxide and binder are so shaped. The mixture is heated to a temperature higher than the boiling point of the binder to evaporate the binder, and the metal oxide powder is sintered in a porous shape to form the porous sintered body 51.
In pressing the mixture of the metal oxide and the binder into a predetermined shape, the mixture is formed in a shape as large as possible to form the porous sintered body 51 as large as possible and accommodated in the oxidation portion accommodation hole 53a. The number of the porous sintered bodies 51 to be reduced is reduced as much as possible (for example, about 2 to 5 pieces). By the way, in this embodiment, the porous sintered body 51 is formed into a cylindrical shape by forming the mixture into a cylindrical shape, and a plurality of the cylindrical porous sintered bodies 51 are stacked to form a whole. The cylindrical portion can be accommodated in the oxidation portion collecting hole 53a.

  That is, by reducing the number of the porous sintered bodies 51 constituting the oxidation part Ox, the handling of the porous sintered bodies 51 is facilitated, the assembly of the hydrogen gas removing device E at the time of manufacture, and the removal of hydrogen gas Maintenance for capacity recovery has been further simplified.

Hereinafter, manufacturing conditions of the porous sintered body 51 will be described.
That is, the particle size of the metal oxide raw material powder, the amount of the binder, the molding pressure of the mixture of the metal oxide powder and the binder, the firing temperature and the firing time, which are the production conditions of the porous sintered body 51, are as follows: Is set to a predetermined value within the range described in.

Particle size of most of the metal oxide raw material powder (for example, 80 wt% or more): 0.05 to 30 μm, preferably 0.1 to 10 μm
Amount of binder: 0.1 to 10 wt%, preferably 1 to 5 wt%
Molding pressure: 2.5 to 147 MPa, preferably 4.9 to 98 MPa
Firing temperature: 400 to 1100 ° C, preferably 500 to 1000 ° C
Firing time: 0.2-6h, preferably 0.5-5h

  FIG. 3 shows an example of the particle size distribution of the raw material powder of the metal oxide (cupric oxide) that forms the porous sintered body 51. In the example shown in FIG. 3, the particle size of about 95 wt% of the raw material powder of metal oxide (cupric oxide) forming the porous sintered body 51 is in the range of 0.1 to 10 μm.

Next, the result of verifying that the hydrogen gas removal capability can be improved by setting the density of the porous sintered body 51 to 4.0 g / cm ³ or more will be described.
In this verification test, the pressure in the storage tank 42 is removed by removing the hydrogen gas by the porous sintered body 51 in a state where the absorption liquid pump 23 is temporarily stopped and the introduction of hydrogen gas into the storage tank 42 is stopped. Is measured for the time required for the pressure to decrease from the upper pressure (for example, 12 kPa) to the lower pressure (for example, 9.33 kPa) (hereinafter, may be referred to as pressure reduction required time), and the measured pressure decrease required time is By comparing, the hydrogen gas removal capability was compared.

In the case of the porous sintered body 51 having a density of 4.0 g / cm ^3, the pressure reduction required time is 4.5 hours, and in the case of the porous sintered body 51 having a density of 6.2 g / cm ³ , The time required for pressure reduction was 4 to 5 hours. Description is omitted, the density even 4.0,6.2g / cm ³ other 4.0 g / cm ³ or more porous sintered body 51, the pressure drop required time has a density of 4.0 g / cm ³ and substantially the same as the porous sintered body 51 of FIG.
Further, in the case of the porous sintered body 51 having a density of 3.0 g / cm ³ , the pressure in the storage tank 42 could be reduced only to 9.80 kPa.

In other words, the density is in the porous sintered body 51 of a small 3.0 g / cm ³ than 4.0 g / cm ^3, since the volumetric efficiency of the metal oxide is small, to sufficiently remove the hydrogen gas in the storage tank 42 By the time, the content of the metal oxide is reduced and the hydrogen gas removal capability is lowered, so that the pressure in the storage tank 42 can be lowered only to 9.80 kPa.

Next, the hydrogen gas removal capacity (cm ³ / h) per hour indicates that the hydrogen gas removal capability can be improved by setting the density of the porous sintered body 51 to 4.0 g / cm ³ or more. The result verified by comparing the will be described.
In this verification test, for each of the porous sintered bodies 51 having different densities, the hydrogen gas per hour when the heating temperature of the porous sintered body 51 is 180 ° C and 210 to 230 ° C, respectively. The removal amount was measured, and the hydrogen gas removal capability was compared by comparing the measured hydrogen gas removal amount per hour.

FIG. 4 shows the relationship between the density of the porous sintered body 51 and the amount of hydrogen gas removed per hour. Incidentally, in FIG. 4, the amount of hydrogen gas removed per hour is measured for each porous sintered body 51 having a density of 3.5 to 6.2 g / cm ³ , and the density is 3.5 to 6.2 from the measurement data. The relationship between the density of the porous sintered body 51 at 6.2 g / cm ³ and the amount of hydrogen gas removed per hour was determined. From this relationship, the density was 3.5 to 6.2 g / cm ^3. The amount of hydrogen gas removed per hour of the porous sintered body 51 other than the above can be estimated.
Incidentally, the standard hydrogen gas removal amount per hour in the conventional hydrogen gas removal apparatus is 45 cm ³ / h.

From FIG. 4, when the density of the porous sintered body 51 is set to 4.0 g / cm ³ or more, it is possible to increase the volume efficiency of the metal oxide and increase the amount of hydrogen gas removed per hour. I understand.
It can also be seen that the amount of hydrogen gas removed per hour is larger when the heating temperature of the porous sintered body 51 is 210 to 230 ° C. than when the heating temperature is 180 ° C.

That is, in the porous sintered body 51 having a density smaller than 4.0 g / cm ³ , the volumetric efficiency of cupric oxide is small, so that the amount of hydrogen gas removed per hour is low, while the density is 4. In the porous sintered body 51 of 0 g / cm ³ or more, the volume efficiency of cupric oxide is increased, so that the amount of hydrogen gas removed per hour is increased.
Furthermore, since the heat conduction of the porous sintered body 51 is increased by setting the density of the porous sintered body 51 to 4.0 g / cm ³ or more, the porous sintering is performed by the electric heater 52 as described above. When the body 51 is heated to the set temperature to perform hydrogen gas removal, the temperature distribution is reduced over the entire porous sintered body 51 and maintained over the entire porous sintered body 51 at a temperature suitable for the reduction reaction. This also increases the amount of hydrogen gas removed per hour.

The short time required for the pressure drop means that the amount of hydrogen gas removed per hour is large. As described above, the hydrogen gas removal capacity is compared by comparing the time required for pressure drop. The time required for pressure drop is short, and the amount of hydrogen gas removed per hour is large when comparing the hydrogen gas removal capacity by comparing the amount of hydrogen gas removed per hour In any case, the removal amount of hydrogen gas per unit volume in the porous sintered body 51 of cupric oxide is large, that is, the hydrogen gas removal ability is high.
That is, it was verified that the hydrogen gas removal ability can be improved by setting the density of the porous sintered body 51 to 4.0 g / cm ³ or more by the above-described two kinds of verification tests. .

Further, as the density of the cupric oxide porous sintered body 51 increases and approaches 6.4 g / cm ³ corresponding to the specific gravity of the cupric oxide crystal, the pores of the porous sintered body 51 become larger. Tends to be finer.
When the density of the cupric oxide porous sintered body 51 is 6.3 g / cm ³ or less, hydrogen gas can be sufficiently infiltrated into the cupric oxide porous sintered body 51, which is high. It can be inferred that hydrogen gas removal capability can be obtained.
That is, in order to further increase the hydrogen gas removal capability, it is preferable to set the density of the cupric oxide porous sintered body 51 in the range of 4.0 to 6.3 g / cm ³ .

As described above, by setting the density of the cuprous oxide porous sintered body 51 to 4.0 g / cm ³ or more and increasing the hydrogen gas removal capability, the volume of the porous sintered body 51 is reduced. While avoiding the increase, for example, the time during which the porous gas 51 can remove the hydrogen gas generated by a predetermined amount per unit time can be increased.
In other words, by setting the density of the cupric oxide porous sintered body 51 to 4.0 g / cm ³ or more, the frequency of maintenance for recovering the hydrogen gas removal capability can be reduced while downsizing the hydrogen gas removal device. It can be lowered and the burden on the maintenance can be reduced.

  For example, every time the operation time of the absorption chiller reaches the set time for maintenance, or every time the accumulated combustion amount of the gas burner 25 of the high-temperature regenerator 3 reaches the set accumulated combustion amount for maintenance, the recovery of the hydrogen gas removal capability is performed. According to the hydrogen gas removal device of the present invention, it is possible to set the maintenance set time longer, or to set the maintenance set integrated combustion amount more, The burden on maintenance for recovering the hydrogen gas removal capability can be reduced.

[Second Embodiment]
Hereinafter, although 2nd Embodiment of this invention is described, in this 2nd Embodiment, since the porous sintered compact 51 differs, it has comprised similarly to 1st Embodiment, Therefore 1st Embodiment and Description of the same components and components having the same action is omitted, and the porous sintered body 51 will be mainly described.
That is, as shown in FIG. 1, the double-effect absorption refrigerator having the hydrogen gas removing device E has the same configuration as that of the first embodiment, and as shown in FIG. 2, the hydrogen gas removing device E Is attached to the storage tank 42 in the same configuration as in the first embodiment.

  As in the first embodiment, the porous sintered body 51 includes a metal oxide (copper oxide in this embodiment) powder and a binder (polyvinyl in this embodiment) having a boiling point lower than that of the metal oxide. The mixture is heated to a temperature higher than the boiling point of the binder to sinter the metal oxide powder into a porous form, and the average pore radius of the porous sintered body 51 is 300 to The range is set to 3000 nm.

  The average pore radius of the porous sintered body 51 is a value measured using a pore distribution measuring device by various measuring methods such as a mercury intrusion method and a gas adsorption method. In this embodiment, Shimadzu Corporation It is a value measured using an auto pore 9220 type pore distribution measuring device by a mercury intrusion method.

  More specifically, as in the first embodiment, the mixture of the metal oxide and the binder is formed into a shape that is as large as possible, and the porous sintered body 51 is formed as large as possible to accommodate the oxidized portion. The number of porous sintered bodies 51 accommodated in the holes 53a is reduced as much as possible (for example, about 2 to 5).

  The production conditions of the porous sintered body 51, ie, the particle size of the metal oxide powder, the amount of the binder, the molding pressure, the firing temperature and the firing time of the mixture of the metal oxide powder and the binder are each porous. In order to set the average pore radius of the sintered body 51 to a predetermined value within the range of 300 to 3000 nm, the average pore radius is set to a predetermined value within the same range as described in the first embodiment.

Next, the result of verifying that the hydrogen gas removal capability can be improved by setting the average pore radius of the porous sintered body 51 in the range of 300 to 3000 nm will be described.
In this verification test, the hydrogen gas removal capability was compared by comparing the time required for pressure drop, as in the first embodiment.

In the case of the porous sintered body 51 having an average pore radius of 1500 nm, the time required for the pressure drop was 6.2 hours. Although not described, even in the porous sintered body 51 having an average pore radius in the range of 300 to 3000 nm other than 1500 nm, the time required for the pressure reduction is substantially the same as that of the porous sintered body 51 having an average pore radius of 1500 nm. It was equivalent.
In the case of the porous sintered body 51 having an average pore radius of 4400 nm, the pressure in the storage tank 42 can be reduced only to 10.1 kPa, and the porous sintered body having an average pore radius of 130 nm. In the case of 51, the pressure in the storage tank 42 could only be reduced to 11.3 kPa.

That is, in the porous sintered body 51 of 4400 nm whose average pore radius is larger than the range of 300 to 3000 nm, since the volume efficiency of the metal oxide is small, until the hydrogen gas in the storage tank 42 is sufficiently removed, The content of the metal oxide is reduced, and the hydrogen gas removal ability is reduced. On the other hand, in the porous sintered body 51 having a mean pore radius smaller than the range of 300 to 3000 nm, the porous sintered body 51 is porous sintered. Since the pores of the body 51 are too fine to allow hydrogen gas to penetrate into the porous sintered body 51, the hydrogen gas removal capability is low, and the hydrogen gas in the storage tank 42 cannot be removed sufficiently.
Therefore, it was verified that the hydrogen gas removal ability can be improved by setting the average pore radius of the porous sintered body 51 in the range of 300 to 3000 nm.

[Another embodiment]
Next, another embodiment will be described.
(A) The installation location of the hydrogen gas removing device E is not limited to the storage tank 42 illustrated in the above embodiments.
For example, as shown in FIG. 5, the suction part 41 and the storage tank 42 installed in each of the above embodiments are omitted, and a hydrogen gas removal device E is provided in the separator 26, or as shown in FIG. The separator 26 may be omitted and provided in the gas phase portion of the high temperature regenerator 3.
In these cases, since the suction part 41 and the storage tank 4 can be omitted, the structure can be simplified and the cost can be reduced.
When the hydrogen gas removing device E is provided in the high temperature regenerator 3, as shown in FIG. 6, it is provided in a portion on the downstream side in the refrigerant vapor flow direction from the interior separator 26a provided in the gas phase portion of the high temperature regenerator 3. Is desirable.
Further, when the hydrogen gas removing device E is provided in the separator 26 or the high temperature regenerator 3, the hydrogen gas removing device E (specifically, the mounting block 53) is installed on the wall of the vessel as in the above embodiments. And a structure for detachably connecting and fixing to the wall of the separator 26 and the high-temperature regenerator 3 in a state of forming a part, and a hydrogen gas removing device E attached to the wall of the separator 26 and the high-temperature regenerator 3 It is desirable that the electric heater 52 be removable from the outside of the separator 26 or the high temperature regenerator 3 without breaking the airtightness of the separator 26 or the high temperature regenerator 3 in the state.

  Further, for example, in each of the above embodiments, the hydrogen gas removing device E may be provided at a plurality of locations, such as by adding the hydrogen gas removing device E to the storage tank 42 and providing the separator 26 or the high temperature regenerator 3.

(B) In the above-described embodiment, the porous sintered body 51 has either a density of 4.0 g / cm ³ or more and an average pore radius of 300 to 3000 nm. The case where the porous sintered body 51 is formed so as to be satisfied is exemplified. Both the density of the porous sintered body 51 is 4.0 g / cm ³ or more and the average pore radius is in the range of 300 to 3000 nm. It may be formed so as to satisfy the above.

(C) The manufacturing method of the porous sintered body 51 is limited to the method exemplified in each of the above embodiments, that is, the method of heating the mixture of the metal oxide powder and the binder to a temperature higher than the boiling point of the binder. Various methods are possible.
For example, a method in which a mixture of a metal powder and a binder is heated to a temperature higher than the boiling point of the binder and the metal is oxidized during the heating process, or a mixture of the metal powder and the binder is heated to the boiling point of the binder. It is possible to sinter metal powder by heating to a higher temperature and oxidize the metal after the sintering.

(D) In each of the above embodiments, the case where the oxidized portion Ox is constituted by a plurality of porous sintered bodies 51 is exemplified. However, the oxidized portion Ox is constituted by one porous sintered body 51. You may do it. In this case, the mixture of the metal oxide and the binder is pressure-molded into a shape slightly smaller than the oxidized portion accommodating hole 53a, and heated to thereby form the porous sintered body 51 into the oxidized portion accommodating hole 53a. The oxidized portion Ox is constituted by one porous sintered body 51 so as to have a shape that can be accommodated in the porous sintered body 51.

(E) In each of the above embodiments, the porous sintered body 51 is illustrated as being formed by sintering only a metal oxide into a porous form. It may be formed by sintering an object into a porous shape. However, if the porous sintered body 51 contains a material other than the metal oxide, the volume efficiency of the metal oxide is reduced. Therefore, it is desirable to reduce the content of the material other than the metal oxide as much as possible.

(F) The specific configuration of the heating means for heating the porous sintered body 51 as the oxidation portion Ox is not limited to the configuration using the electric heater 52 exemplified in each of the above embodiments as a heat source. Various configurations such as a configuration using the combustion exhaust gas of the gas burner 25 of the high-temperature regenerator 3 as a heat source are possible.

(G) The metal oxide that forms the porous sintered body 51 is not limited to the cupric oxide exemplified in the above embodiments, but is nickel monoxide (NiO), cobalt monoxide (CoO). ), Chromium oxide, iron oxide, molybdenum oxide, lead oxide, manganese oxide, aluminum oxide, etc., any metal oxide may be used as long as it can oxidize hydrogen gas by a reduction reaction to make it condensable.
In addition, when using nickel monoxide as a metal oxide which forms the porous sintered compact 51, the density of the porous sintered compact 51 of the nickel monoxide is the range of 5.0-6.5 g / cm < ³ >. In addition, when cobalt monoxide is used as the metal oxide forming the porous sintered body 51, the density of the porous sintered body of cobalt monoxide is 4.0 to 6.2 g / cm ^3. The range of is preferable.
In addition, the binder to be mixed with the metal oxide powder to form the porous sintered body 51 is not limited to the polyvinyl alcohol exemplified in each of the above embodiments. For example, salicylic acid, camphor ( It is possible to use metal salts such as C ₁₀ H ₁₆ O, bicyclic saturated terpene ketone) and stearic acid.

(H) The specific example of the apparatus for removing hydrogen gas is not limited to the double-effect absorption refrigerator as exemplified in the above embodiment.
For example, when the hydrogen gas removal target device is an absorption refrigerator, a single effect or triple effect may be used in addition to the double effect as in the above embodiment. In addition to the combination of water and lithium bromide as in the above embodiment, various combinations of refrigerant and absorbent, such as a combination of ammonia and water, are possible as the combination of the refrigerant and the absorbent.
In addition to the absorption refrigerator, various devices that generate hydrogen gas in the device can be targeted for hydrogen gas removal by the hydrogen gas removal device of the present invention.

Configuration diagram of an absorption chiller equipped with a hydrogen gas removal device according to an embodiment The longitudinal cross-sectional view which shows the hydrogen gas removal apparatus which concerns on embodiment, and its attachment structure The figure which shows the distribution of the particle size of the raw material powder of the metal oxide which forms the porous sintered body The figure which shows the relationship between the density and hydrogen gas removal capability in the porous sintered compact of cupric oxide The block diagram of the absorption refrigerator provided with the hydrogen gas removal apparatus which concerns on another embodiment The block diagram of the absorption refrigerator provided with the hydrogen gas removal apparatus which concerns on another embodiment

Explanation of symbols

51 Oxidation part of porous sintered body Ox

Claims (8)

A hydrogen gas removing device configured to oxidize and remove hydrogen gas generated in a device of a hydrogen gas removal target device in an oxidation unit containing a metal oxide,
The hydrogen gas removal apparatus in which the said oxidation part is comprised with the porous sintered compact of the metal oxide.   In the porous sintered body, a mixture of a metal oxide powder and a binder having a boiling point lower than that of the metal oxide is heated to a temperature higher than the boiling point of the binder to sinter the metal oxide powder into a porous form. The hydrogen gas removing device according to claim 1, wherein the hydrogen gas removing device is formed by bonding. The hydrogen gas removing device according to claim 1 or 2, wherein the metal oxide is cupric oxide (CuO), and the density of the porous sintered body of the cupric oxide is 4.0 g / cm ³ or more. The hydrogen gas according to claim 1 or 2, wherein the metal oxide is nickel monoxide (NiO), and the density of the porous sintered body of nickel monoxide is in the range of 5.0 to 6.5 g / cm ^3. Removal device. ^3. The hydrogen gas according to claim 1, wherein the metal oxide is cobalt monoxide (CoO), and the density of the porous sintered body of cobalt monoxide is in the range of 4.0 to 6.2 g / cm ^3. Removal device.   3. The hydrogen gas removing device according to claim 1, wherein an average pore radius of the porous sintered body is in a range of 300 to 3000 nm.   The hydrogen gas removal apparatus according to any one of claims 1 to 6, wherein a particle size of most of the metal oxide raw material powder forming the porous sintered body is in a range of 0.1 to 10 µm. .   The hydrogen gas removal device according to any one of claims 1 to 7, wherein the hydrogen gas removal target device is an absorption refrigerator.

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