JP7274882B2 - catalyst vessel - Google Patents

Description

The present invention relates to catalyst vessels.

Patent Literature 1 discloses a fuel reforming system that generates fuel gas to be supplied to a fuel cell. A fuel reforming system has a gas treatment device that receives supply of a gas to be treated, which is a raw fuel, and performs a predetermined treatment on the gas to be treated using a catalyst. The catalyst is housed in the gas treatment device, and as the device is repeatedly started and stopped, the member forming the space housing the catalyst expands and contracts, and the granular catalyst housed in the space is crushed and finely divided. become When the finely divided finely divided catalyst accumulates in the gaps between the granular catalysts, the flow of the gas to be treated is hindered.

Therefore, in the gas treatment apparatus of Patent Document 1, the catalyst accommodation space is divided into an upper catalyst accommodation portion for accommodating granular catalyst and a lower finely divided catalyst accommodation portion for accommodating finely divided catalyst. Then, the catalyst in the catalyst housing space is vibrated by the vibrating means while the supply of the gas to be processed to the catalyst housing space is stopped. This prevents the finely divided catalyst from flowing downstream along with the flow of the gas to be treated, and allows the finely divided catalyst accumulated between the granular catalysts to be sifted into the finely divided catalyst accommodating portion. . Therefore, it is possible to sufficiently suppress the occurrence of drift in the gas to be treated flowing through the catalyst housing space.

Japanese Patent No. 6381458

In the gas treatment apparatus of Patent Document 1, although the finely divided catalyst can be sifted into the lower portion containing the finely divided catalyst, the flow path through which the gas to be treated flows and which is connected to the lower part of the gas treatment apparatus is not finely divided. It may be clogged by a catalyst or the like. Therefore, the gas to be treated cannot be allowed to flow through the catalyst housing space and may not be subjected to treatment by the catalyst.

SUMMARY OF THE INVENTION Accordingly, it is an object of the present invention to provide a catalyst container capable of providing countermeasures against clogging of a flow path for supplying a gas to be treated to a catalyst housing space.

The characteristic configuration of the catalyst container according to the present invention is
A catalyst container containing a granular catalyst and through which a gas to be treated can flow,
a container body through which the gas to be treated flows from below to above;
a plurality of supply channels connected to the lower surface of the container body and capable of supplying the gas to be processed to the container body;
The container body is
an introduction part to which the supply channel is partially connected and into which the gas to be processed is introduced;
a catalyst containing portion positioned above the introducing portion and containing the granular catalyst;
a partition that separates the introducing portion and the catalyst containing portion;
The partition body has a plurality of openings that prevent the granular catalyst from falling into the introduction part and allows the gas to be treated to pass from the introduction part to the catalyst storage part,
The plurality of supply channels includes at least a first supply channel that can be switched between opening and closing by a first plug, and a second supply channel that can be switched between opening and closing by a second plug. fruit,
The first supply channel and the second supply channel have a first threaded portion and a second threaded portion,
The first plug can be screwed onto the first threaded portion,
The second plug can be screwed onto the second threaded portion,
The first plug body and the second plug body are cap nut-like nuts closed on the opposite side to the side to be screwed together.

The gas to be processed is introduced into the introduction section from below the container body through the supply channel. The gas to be treated introduced into the introduction part passes through the plurality of openings of the partition body, is introduced into the catalyst storage part, and is subjected to a predetermined treatment by the catalyst. In this way, the target gas is introduced from the supply channel into the introduction part and the catalyst containing part, and the target gas is swirled in the introduction part due to contact with the partition body and the inner wall of the introduction part. sometimes. When the generated swirling flow passes through the plurality of openings of the partition and is introduced into the catalyst storage section, the powder particles are rolled up and dropped into the introduction section through the plurality of openings of the partition, and the supply flow block the road. Examples of the powder include a subdivided catalyst obtained by subdividing a catalyst, and a reaction product between a granular catalyst and a gas to be treated. When the device provided with the catalyst container is started and stopped, the catalyst container is subjected to expansion and contraction forces, which causes the catalyst accommodated in the catalyst container to be crushed and fragmented into fragmented catalysts.

According to the above characteristic configuration, the catalyst container is provided with at least the first and second supply channels capable of supplying the gas to be treated to the container body, and the first and second plugs are used to open the respective channels. and closing can be switched. Therefore, when one of the supply channels is clogged with powder, the supply channel is closed and the other supply channel is opened to supply the target gas to the container body.
By providing at least the first and second supply channels, when one of the supply channels is blocked, the opening and closing of the first and second supply channels are switched to continue the gas to be processed. It can be supplied to the container body.
Moreover, according to the above characteristic configuration, the first and second plugs can be screwed into the first and second supply channels via the first and second threaded portions. Therefore, the first and second plugs can be used to open and close the first and second supply channels.

A further characteristic configuration of the catalyst container according to the present invention is
The plurality of supply channels are arranged side by side at predetermined intervals in order from the end of the container body when viewed in the vertical direction.

When a plurality of supply channels are provided adjacent to each other at one location, if one supply channel is blocked by powder particles, the other adjacent supply channels are similarly blocked by powder particles. It is very likely that you will. According to the above-described characteristic configuration, since the plurality of supply channels are arranged in order from the end of the container body at predetermined intervals, even if one supply channel is blocked by powder particles, other supply channels can be supplied. It is possible to reduce the possibility of particles entering the flow path. Therefore, when any of the supply channels is blocked, the gas to be processed can be continuously supplied to the container main body by switching between opening and closing of the first and second supply channels.

A further characteristic configuration of the catalyst container according to the present invention is
The first threaded portion of the first supply channel and the second threaded portion of the second supply channel have the same shape,
The first plug can be screwed into any of the first and second supply channels, and the second plug can be screwed into any of the first and second supply channels. at some point.

According to the above characteristic configuration, the first plug that can switch between opening and closing of the first supply channel can also be used to close the second supply channel. Similarly, the second plug that can switch between opening and closing of the second supply channel can also be used to close the first supply channel. In other words, regardless of which supply channel it is, it can be closed by applying the plug.

It is a block diagram which shows the whole structure of a gas treatment apparatus. It is a perspective view which shows the whole structure of a catalyst container. FIG. 4 is a side view of the catalyst container from +X and −X directions; FIG. 4 is a side view of another catalyst container from the +X and −X directions; FIG. 3 is a configuration diagram of a catalyst container; FIG. 4 is an explanatory diagram showing how supply channels are switched; 1 is a perspective view showing the overall configuration of a conventional catalyst container; FIG. FIG. 10 is an explanatory diagram showing the difference in temperature distribution when gas to be treated is introduced into a conventional catalyst vessel at different flow velocities; FIG. 10 is an explanatory diagram showing differences in velocity vectors when target gases are introduced into a conventional catalyst vessel at different flow velocities; FIG. 10 is an explanatory diagram showing the difference in trajectories when a gas to be treated is introduced into a conventional catalyst container at different flow velocities;

[Embodiment]
BEST MODE FOR CARRYING OUT THE INVENTION An embodiment in which a catalyst container according to the present invention is applied to a gas treatment apparatus for generating hydrogen-containing gas (fuel gas) will be described below with reference to the drawings.

(1) Overall Configuration of Gas Treatment Apparatus The overall configuration of the gas treatment apparatus 10 will be described with reference to FIG. As shown in FIG. 1, a gas treatment apparatus 10 for generating a hydrogen-containing gas includes a hydrocarbon-based raw fuel gas (for example, a natural gas-based city gas such as 13A) as a treatment unit that performs a predetermined treatment on a gas to be treated. a desulfurizer 11 for desulfurizing the gas); a reformer 13 for reforming the desulfurized raw fuel gas supplied from the desulfurizer 11 to generate a reformed gas; It comprises a CO shift converter 15 for converting carbon oxide gas into carbon dioxide gas, and a CO selective oxidation reactor 17 for selectively oxidizing carbon monoxide gas contained in the reformed gas.
In this embodiment, the raw fuel gas contains sulfur, and the desulfurizer 11 is provided to desulfurize the raw fuel gas.

The desulfurizer 11, the reformer 13, the CO shift converter 15, and the CO selective oxidation reactor 17 each include a catalyst vessel 30 (see FIG. ). The configuration of the catalyst container 30 will be described later. The configuration of the connecting pipes of the desulfurizer 11, the reformer 13, the CO shift converter 15 and the CO selective oxidation reactor 17 in FIG. 1 is simplified.

A desulfurization catalyst 11c for desulfurization is accommodated in the catalyst accommodation portion Ru of the desulfurizer 11 .
Then, the desulfurizer 11 desulfurizes the raw fuel gas while raising the temperature of the desulfurization catalyst 11c to a predetermined desulfurization treatment temperature (for example, 200 to 270° C.) for desulfurization treatment. In this case, part of the reformed gas that has passed through the reformer 13 may be supplied to the desulfurizer 11 as recycled gas. As a result, the sulfur compounds in the raw fuel gas are hydrogenated by the hydrogen gas in the recycle gas, and the desulfurization catalyst 11c adsorbs and desulfurizes the hydrides. The desulfurization catalyst 11c is formed by supporting a catalytic substance such as nickel, cobalt, molybdenum, copper, zinc, aluminum, chromium, etc., on a porous granular body made of ceramic or the like.

The reformer 13 accommodates a reforming catalyst 13c for reforming in the catalyst accommodating portion Ru.
The reformer 13 is supplied with the raw fuel gas after desulfurization by the desulfurizer 11 and also with steamed reforming water. The reformer 13 steam-reforms the raw fuel gas after desulfurization while raising the temperature of the reforming catalyst 13c to a predetermined reforming process temperature (for example, in the range of 600 to 700° C.). .
When the raw fuel gas is natural gas containing methane gas as a main component, the reformer 13 reacts the methane gas with water vapor according to the following reaction formula to reform the gas, thereby generating a reformed gas. In the reaction formula below, the reformed gas includes hydrogen gas, carbon monoxide gas and carbon dioxide gas. The reforming catalyst 13c is formed by supporting a catalytically active substance such as ruthenium, nickel, platinum, etc., on a porous granular body made of ceramic or the like.

_CH4 + _2H2O → _CO2 + _4H2
CH4 + _H2O →CO+ _3H2

The catalyst accommodating portion Ru of the CO shift converter 15 accommodates a shift conversion catalyst 15c for shift conversion processing.
The CO shift converter 15 converts carbon monoxide in the reformed gas according to the following reaction formula while the temperature of the shift conversion catalyst 15c is raised to a predetermined shift conversion temperature (for example, 150 to 250° C.) for the shift conversion. The gas is reacted with water vapor and transformed into carbon dioxide gas. Note that the shift conversion catalyst 15c is formed by supporting a catalytically active substance such as platinum, ruthenium, rhodium, etc. on a porous granular body made of ceramic or the like.

CO+ _H2O → _CO2 + _H2

A selective oxidation catalyst 17c for selective oxidation treatment is accommodated in the catalyst accommodating portion Ru of the CO selective oxidation reactor 17 .
In the CO selective oxidation reactor 17, in a state where the selective oxidation catalyst 17c is heated to a predetermined selective oxidation treatment temperature (for example, in the range of 80 to 100° C.), selectively oxidize the remaining carbon monoxide gas. Thereby, the CO selective oxidation reactor 17 produces a hydrogen-containing gas (fuel gas) that can be supplied to the fuel cell 20 . The hydrogen-containing gas is produced as a hydrogen-rich hydrogen-containing gas with a low carbon monoxide gas concentration (for example, 10 ppm or less). The selective oxidation catalyst 17c is formed by supporting a catalytically active substance such as platinum, ruthenium, rhodium, etc. on a porous granular body made of ceramic or the like.

The hydrogen-containing gas leaving the CO selective oxidation reactor 17 is supplied to the fuel cell 20 . The fuel cell 20 reacts the supplied hydrogen-containing gas with air to generate electricity. The fuel cell 20 is not particularly limited as long as it can generate electricity using a hydrogen-containing gas as a fuel gas. shape fuel cell.

(2) Catalyst Container Next, the catalyst container 30 will be described. As described above, each of the desulfurizer 11, reformer 13, CO shift converter 15, and CO selective oxidation reactor 17 has a catalyst container 30. Predetermined catalysts 11c, 13c, 15c, and 17c are accommodated. Since the structure of the catalyst container 30 is the same in each processing section, the catalyst container 30 of the desulfurizer 11 will be described below as an example.

As shown in FIGS. 2 and 3, the catalyst container 30 of the desulfurizer 11 is connected to a container main body R through which the gas to be treated flows upward and to the lower surface of the main body R, so that the gas to be treated flows. and a supply channel 31 for supplying to the container body. The catalyst container 30 may further have a discharge passage 39 connected to the upper surface of the container body R for discharging the treated gas that has undergone a predetermined treatment with the catalyst.

In this embodiment, the container main body R has a rectangular parallelepiped shape. The longitudinal direction of the container body R is the +X and -X directions (hereinafter sometimes referred to as the width direction) in FIGS. 2, 3, etc., and the length in the longitudinal direction is L2. The +Y and -Y directions (hereinafter sometimes referred to as the depth direction) are the widthwise directions, and the length in the widthwise direction is W1 (L2>W1). The +Z and -Z directions (hereinafter also referred to as vertical directions) are height directions. Hereinafter, a plane including +X and -X directions and +Y and -Y directions is defined as a horizontal plane, and a direction along the horizontal plane is defined as a horizontal plane direction. The shape of the container main body R in the horizontal direction is generally rectangular.

The container body R includes a partition body 41 that vertically partitions the space inside the container body R, and a rectangular parallelepiped space above the partition body 41, and a catalyst containing portion Ru that contains a desulfurization catalyst 11c that is a granular catalyst. and an introduction portion Rb, which is a rectangular parallelepiped space below the partition 41 and to which the supply flow path 31 is connected. The catalyst housing portion Ru has a length L1 in the +X and -X directions, which are longitudinal directions, and a length W1 (L1>W1) in the +Y and -Y directions, which are lateral directions, and the height is arbitrary. , for example greater than L1 and W1. The introducing portion Rb has a longitudinal length L1, a lateral length W1 (L1>W1), and a height L8 smaller than L1. The catalyst containing portion Ru is formed in a space wider than that of the introducing portion Rb, and is capable of containing a larger amount of catalyst.

The partition 41 is made of a plate-like member and has a plurality of holes (an example of an opening) 43 . The plurality of holes 43 are sized to prevent the granular catalyst accommodated in the catalyst containing portion Ru from falling into the introduction portion Rb and to allow the gas to be treated to pass from the introduction portion Rb to the catalyst containing portion Ru. It is
In addition, the catalyst containing portion Ru is formed in a space wider than that of the introduction portion Rb, and is capable of containing a larger amount of catalyst.

The supply channel 31 (31a, 31b, 31c) is a cylindrical member and communicates with the lower surface of the introduction portion Rb via a connecting portion. In addition, the supply channel 31 extends in the +Z and -Z directions (vertical direction) at least in the vicinity of the connecting portion with the introduction portion Rb. The supply channel 31 is connected to the introduction part Rb so that the gas to be processed introduced from below the supply channel 31 is blown upward toward the introduction part Rb. The supply channels 31 (31a, 31b, 31c) will be described in detail later.

Further, in the present embodiment, as shown in FIG. 3, the lower surface of the introduction portion Rb is a horizontal plane having the same height in the direction from -Y to +Y. However, as shown in FIG. 4, the lower surface of the introduction portion Rb may be inclined so that the height increases from the -Y direction to the +Y direction. This makes it easy to connect the supply channel 31 to the lower surface of the introduction portion Rb by welding or the like.

Here, the gas to be processed is introduced from the supply flow path 31 into the introduction portion Rb and the catalyst containing portion Ru, and is processed in the introduction portion Rb by contact with the partition body 41 and the inner wall of the introduction portion Rb. A swirling flow of the target gas may occur. Then, when the gas to be processed comes into contact with the partition body 41 and the inner wall of the introduction part Rb, etc. at a relatively high flow velocity, a swirl flow is likely to occur. When the generated swirling flow passes through the plurality of holes 43 of the partition 41 and is introduced into the catalyst housing portion Ru, the powder particles are rolled up and dropped through the plurality of holes 43 of the partition 41 into the introduction portion Rb. to close the supply channel 31 . Examples of the powder include a subdivided catalyst obtained by subdividing a catalyst, and a reaction product between a granular catalyst and a gas to be treated. In the desulfurizer 11, copper sulfide is produced as a reactant.
When the device provided with the catalyst container 30 is started and stopped, the catalyst container 30 is subjected to expansion and contraction forces. becomes.

The catalyst container 30 of the present embodiment is provided with a plurality of first to third supply channels 31a, 31b, 31c (31). Therefore, when one of the supply channels 31 is blocked by powder particles, the supply channel 31 is closed, and the other supply channel 31 is opened to supply the target gas to the container body R. . By providing the plurality of first to third supply channels 31a to 31c in this way, when any of the supply channels 31 is blocked, the plurality of first to third supply channels 31a to 31c can be opened. The gas to be treated can be continuously supplied to the container main body R by switching between the stopper and the closed stopper. Therefore, countermeasures can be provided when the supply channel 31 is blocked.

The catalyst container 30 having the three first to third supply channels 31a to 31c will be further described below. As shown in FIGS. 2, 5, and 6, three vertically extending first to third supply flow paths 31a to 31c are connected to the lower surface of the introduction portion Rb. In the state of FIG. 5, the gas to be processed is introduced from the first supply channel 31a into the introduction portion Rb, and the gas to be processed is not supplied from the second and third supply channels 31b and 31c. In this case, the first supply channel 31a is opened by removing the first nut 32a, so that the gas to be processed can be supplied to the introduction part Rb. On the other hand, the second and third supply channels 31b and 31c are closed by second and third nuts 32b and 32c, respectively. A supply pipe for the gas to be processed is connected to the unplugged first supply channel 31a by a joint (not shown), and the gas to be processed is supplied from the supply pipe to the first supply channel 31a. .

In this state, if the first supply channel 31a is blocked by powder particles, the first supply channel 31a is closed by the first nut 32a. Instead, one of the second and third supply channels 31b and 31c is opened and used for supplying the gas to be processed. In the case of FIG. 6, when the first supply channel 31a is blocked, a joint (not shown) is removed, the first supply channel 31a is removed from the supply pipe, and the first nut 32a is attached to close the plug. Then, the second nut 32b closing the second supply channel 31b is removed to open the second supply channel 31b. The unplugged second supply channel 31b is connected to the above-described supply pipe for the gas to be processed by a joint (not shown), the gas to be processed is supplied from the supply pipe to the second supply channel 31b, and the gas to be processed is supplied from the second supply channel 31b. Switching is performed so that the gas to be processed is supplied to the introduction part Rb.

The first supply channel 31a has a first male threaded portion (threaded portion) 33a whose outer periphery is threaded. A first nut (plug) 32a can be attached. A first female threaded portion 32a1 is formed on the inner periphery of the first nut 32a to be screwed with the first male threaded portion 33a. Similarly, the second and third supply channels 31b and 31c have second and third male threaded portions (threaded portions) 33b and 33c whose outer circumferences are threaded. Second and third nuts 32b and 32c (plugs) for opening and closing the second and third supply channels 31b and 31c can be attached to the second and third male screw portions 33b and 33c. be. Second and third female threaded portions 32b1 and 32c1 that screw together with the second and third male threaded portions 33b and 33c are formed on the inner peripheries of the second and third nuts 32b and 32c. The first to third nuts 32a to 32c are closed on the side opposite to the side to be screwed with the first to third supply passages 31a to 31c. Therefore, the first to third nuts 32a to 32c are formed like cap nuts.

As a mode of opening and closing by such first to third supply flow paths 31a to 31c and first to third nuts 32a to 32c, the nut 32 is removed from any one of the supply flow paths 31 to open. A mode in which the supply channel 31 is plugged and the rest of the supply channel 31 is closed with a nut 32 is exemplified. For example, as described above, the first supply channel 31 is opened with the first nut 32a removed and connected to a separate supply pipe, and the remaining second and third supply channels 31b and 31c are connected to the second , and the third nuts 32b and 32c.

Further, instead of opening only one supply channel 31, two supply channels 31 can be opened. For example, the first and second supply channels 31a and 31b are opened with the first and second nuts 32a and 32b removed, and connected to a separate supply pipe in common, and the remaining third supply channel 31c is connected. may be closed by the third nut 32c. Thereby, the gas to be processed can be supplied to the introduction part Rb from the two supply flow paths 31 .

As shown in FIGS. 2, 5 and 6, the first to third supply channels 31a to 31c are arranged in order from the end of the introduction portion Rb of the container main body R at predetermined intervals. That is, the first supply channel 31a is connected to the -X direction side of the central portion of the introduction portion Rb in the horizontal direction. More specifically, in the +X and -X directions, the introduction portion Rb has a length of L1, and the first supply channel 31a is located at a position of length L2 from the end on the -X direction side, and in the +X direction. It is connected to the introduction part Rb at the position of the length L3 from the side end. L3 is greater than L2 (L3>L3). The second supply channel 31b is arranged on the +X direction side of the first supply channel 31a, at a position of length L4 from the end on the -X direction side, and by a length from the end on the +X direction side. It is connected to the lead-in portion Rb at the position of L5. L4 is greater than L2 (L4>L2). The third supply channel 31c is arranged on the +X direction side of the second supply channel 31b, is located at a position of length L6 from the end on the -X direction side, and has a length of L6 from the end on the +X direction side. It is connected to the lead-in portion Rb at the position of L7. L6 is greater than L4 (L6>L4).

In the case where a plurality of supply channels 31 are provided adjacently at one location, if one supply channel 31 is blocked by powder particles, the powder particles are also present in the other adjacent supply channels 31 in the same manner. There is a high possibility that it will get in and become blocked. As described above, the plurality of first to third supply channels 31a to 31c are arranged in order from the end of the container body R at predetermined intervals, so that one supply channel 31 is blocked by powder particles. Even in this case, it is possible to reduce the possibility of particles entering other supply channels 31 . Therefore, when any of the supply channels 31 is blocked, the gas to be processed can be continuously supplied to the container main body R by switching between opening and closing of the supply channels 31 .

In the above description, the first to third supply channels 31a to 31c are opened and closed by the first to third nuts 32a to 32c, respectively. However, the first to third nuts 32a to 32c may be commonly used for the first to third supply channels 31a to 31c. For example, the threading structure of the first to third male screw portions 33a to 33c of the first to third supply channels 31a to 31c is the same, and the first to third female screws of the first to third nuts 32a to 32c are the same. The structures of the portions 32a1 to 32c1 are also the same. Therefore, any one of the first to third nuts 32a to 32c may be threadable with the first to third supply passages 31a to 31c.

In the above description, the configuration in which the catalyst container 30 is provided with the three supply channels 31 is described, but the number of the supply channels 31 may be two or more.

(3) Experimental Results In the following, experimental results using the conventional catalyst container 60 for the state where the supply channel 31 is blocked will be described.
The swirling flow is likely to occur when the gas to be processed introduced from the supply channel 31 into the introduction portion Rb comes into contact with the partition 41 and the inner wall of the introduction portion Rb at a relatively high flow velocity. When the generated swirling flow passes through the plurality of holes 43 of the partition 41 and is introduced into the catalyst housing portion Ru, the powder particles are rolled up and dropped through the plurality of holes 43 of the partition 41 into the introduction portion. , to block the supply channel.

FIG. 7 shows the configuration of the catalyst container 60 of the conventional desulfurizer 11. As shown in FIG. A conventional catalyst container 60 includes a partition 71 having a plurality of holes 73 , a catalyst containing portion Ru containing a desulfurization catalyst 11 c , an introduction portion Rb, a supply channel 61 and a discharge channel 69 . In the conventional catalyst container 60, unlike the catalyst container 30 of the present embodiment, which has a plurality of first to third supply channels 31a to 31c, one supply channel 61 extends in the vertical direction. It is connected to the introduction portion Rb on the X direction side. Moreover, the partition 71 is formed along the horizontal plane, and the height between the lower surface of the partition 71 and the upper surface of the introduction portion Rb is constant.

FIG. 8 is a front view of the conventional catalyst container 60 in FIG. It shows the temperature distribution when gas is introduced. The catalyst in the catalyst container 60 is heated to a predetermined processing temperature, and the low-temperature gas to be processed is introduced from the supply passage 61 into the introduction portion Rb and the catalyst containing portion Ru.
As shown in FIG. 8, the case where the gas to be processed is introduced from the supply passage 61 into the introduction portion Rb and the catalyst containing portion Ru at a gas flow rate of 2.65 L/min is higher than the case where the gas flow rate is 1.0 L/min. It can be seen that the spread of the temperature distribution of the low temperature is also large. That is, as the flow rate increases, the target gas is introduced into the catalyst housing portion Ru at a high flow velocity, and the contact resistance between the target gas and the partition member 41 and the introduction portion Rb increases, which may cause a swirling flow. I know it's expensive.

FIG. 9 is a side view of the conventional catalyst container 60, in which the gas to be treated is introduced from the supply channel 61 into the introduction portion Rb and the catalyst containing portion Ru at a gas flow rate of 2.65 L/min and a gas flow rate of 1.0 L/min, respectively. It shows the velocity vector when In FIG. 9, as shown in FIG. 4, a catalyst container is used in which the lower surface of the introduction portion Rb is inclined so that the height increases in the direction from -Y to +Y.

Although the gas to be processed is introduced from the supply channel 61 into the introduction portion Rb, when the gas flow rate is 2.65 L/min, the portion of the region A where the flow velocity is high collides vigorously toward the partition 71, A swirling flow is generated in regions B and C. FIG. On the other hand, when the gas flow rate is 1.0 L/min, the gas to be processed in the region A is directed toward the partition 71, but the flow velocity is slow and the impact with the partition 71 is small. Therefore, almost no swirling flow occurs in the regions B and C.

FIG. 10 is a front view of the conventional catalyst container 60 in FIG. 7, showing a gas flow rate of 2.65 L/min and a gas flow rate of 1.0 L/min, respectively, from the supply flow path 61 to the introduction part Rb and the catalyst storage part Ru. It shows the trajectory when the gas is introduced.
Although the gas to be processed is introduced from the supply channel 61 into the introduction portion Rb, when the gas flow rate is 2.65 L/min, the portion of the region A where the flow velocity is high collides vigorously toward the partition 71, A swirling flow is generated in the region D. In the region E, the space of the introduction part Rb is wider than in the region D in the +X and -X directions, and the contact resistance between the gas to be processed and the introduction part Rb is small. Therefore, no swirling flow is generated in the region E.

On the other hand, when the gas flow rate is 1.0 L/min, the gas to be processed in the region A is directed toward the partition 71, but the flow velocity is slow and the impact with the partition 71 is small. Therefore, almost no swirling flow occurs in region D. Even in region E, which is wider than region D, almost no swirling flow occurs.

From the above experimental results, the clogging of the supply channel 31 is facilitated by increasing the gas flow rate. By adopting the configuration of the present embodiment and providing an alternative supply channel 31, even if one supply channel 31 is blocked, the other supply channel 31 can be used to continue supplying the gas to be processed. Do you get it.

[Other embodiments]
The configurations disclosed in the above-described embodiments (including other embodiments, the same shall apply hereinafter) can be applied in combination with configurations disclosed in other embodiments unless there is a contradiction. The embodiments disclosed in this specification are examples, and the embodiments of the present invention are not limited thereto, and can be modified as appropriate without departing from the scope of the present invention.

(1) In the above embodiment, the catalyst containers 30 of the desulfurizer 11, reformer 13, CO shift converter 15 and CO selective oxidation reactor 17 have the same configuration. However, at least one of the desulfurizer 11, the reformer 13, the CO shift converter 15, and the catalyst container 30 of the CO selective oxidation reactor 17 may employ the configuration described in the above embodiment.

(2) In the above embodiment, the catalyst container 30 has a rectangular parallelepiped shape, but the shape of the catalyst container 30 is not limited to this as long as a plurality of supply channels 31 can be provided. For example, the catalyst container 30 may be square, cylindrical, elliptical, and the like.

Further, in the above embodiment, three first to third supply channels 31a to 31c are provided, but the number of supply channels 31 is not limited to this, and may be two or four. or more. The connection position of the introduction part Rb of the supply channel 31 is not limited to the above embodiment as long as a plurality of supply channels 31 can be provided.

Further, in the above embodiment, the discharge channel 39 is connected to the upper surface of the catalyst container 30 . However, the connection position of the discharge flow path 39 is not limited to this as long as the gas that has undergone a predetermined treatment in the catalyst container 30 can be discharged. For example, the discharge channel 39 may be connected to the upper side surface of the catalyst container 30 or the like.

(3) In the above embodiment, in order to open and close the first to third supply channels 31a to 31c, the first to third male screw portions 33a to 33a 33c are formed, and first to third female screw portions 32a1 to 32c1 are formed on the inner circumferences of the first to third nuts 32a to 32c. However, first to third female screw portions are formed on the inner periphery of the first to third supply flow paths 31a to 31c, and the first to third male screw portions 33a are screwed into the first to third female screw portions. 33c may be formed on the outer periphery of the screw member (plug).

In addition , the timing of opening and closing the plug is not particularly limited, but the timing is when a predetermined time has passed since the start of operation, and when the first to third supply flow paths 31a to 31c are in a closed or nearly closed state. For example, when an error occurs.

(4) In the above embodiments, the polymer electrolyte fuel cell was taken as an example of the fuel cell. However, the fuel cell 20 may be a solid oxide fuel cell constructed by stacking cells in which a ceramic film such as a zirconia-based or selenium-based ceramic film is sandwiched between an anode and a cathode.

(5) In the above embodiment, the desulfurizer 11 is provided. However, the desulfurizer 11 may be omitted from the gas treatment device 10 when a hydrocarbon-based gas such as propane, alcohol, or the like, which does not contain sulfur, is used as the raw fuel. Therefore, in the above embodiment, the processing section of the gas treatment device 10 can also be composed of the reformer 13 , the CO shift converter 15 and the CO selective oxidation reactor 17 .

Furthermore, when the concentration of carbon monoxide contained in the reformed gas after steam reforming is low, the CO shift converter 15 may be omitted from the gas treatment device 10 . Therefore, in the above embodiment, the processing section of the gas treatment device 10 can also be composed of the reformer 13 and the CO selective oxidation reactor 17 .

(6) The gas treatment apparatus 10 of the above embodiment may be provided with a steam condensation separator (not shown) between the CO shift converter 15 and the CO selective oxidation reactor 17 . The steam condensing separator condenses and separates the steam contained in the reformed gas steam-reformed in the reformer 13 to remove it. By removing water vapor, clogging of the lines connecting the processing units can be suppressed.

Also, part of the reformed gas from which water vapor has been removed through the water vapor condensation separator may be mixed with the raw fuel gas. Also, part of the reformed gas reformed through the reformer 13 may be mixed with the raw fuel gas. Also, part of the gas that has passed through the CO transformer 15 may be mixed with the raw fuel gas. Furthermore, part of the gas that has passed through the CO selective oxidation reactor 17 may be mixed with the raw fuel gas.

(7) When the raw fuel gas used in the gas treatment apparatus 10 of the above embodiment is gas and requires compression, a compressor may be provided upstream of the desulfurizer 11 .

11c to 17c: catalyst 30: catalyst container 31: supply flow paths 31a to 31c: first to third supply flow paths 32a to 32c: first to third nuts 32a1 to 32c1: first to third female screw portions 33a to 33c: first to third male screw portions 41: partition body 43: hole Rb: introduction portion Ru: catalyst containing portion

Claims (3)

A catalyst container containing a granular catalyst and through which a gas to be treated can flow,
a container body through which the gas to be treated flows from below to above;
a plurality of supply channels connected to the lower surface of the container body and capable of supplying the gas to be processed to the container body;
The container body is
an introduction part to which the supply channel is partially connected and into which the gas to be processed is introduced;
a catalyst containing portion positioned above the introducing portion and containing the granular catalyst;
a partition that separates the introducing portion and the catalyst containing portion;
The partition body has a plurality of openings that prevent the granular catalyst from falling into the introduction part and allows the gas to be treated to pass from the introduction part to the catalyst storage part,
The plurality of supply channels includes at least a first supply channel that can be switched between opening and closing by a first plug, and a second supply channel that can be switched between opening and closing by a second plug. fruit,
The first supply channel and the second supply channel have a first threaded portion and a second threaded portion,
The first plug can be screwed onto the first threaded portion,
The second plug can be screwed onto the second threaded portion,
The catalyst container , wherein the first plug and the second plug are cap nut-like nuts closed on opposite sides to threads . 2. The catalyst container according to claim 1, wherein said plurality of supply channels are arranged side by side at predetermined intervals in order from the end of said container main body when viewed in a vertical direction. The first threaded portion of the first supply channel and the second threaded portion of the second supply channel have the same shape,
The first plug can be screwed into any of the first and second supply channels, and the second plug can be screwed into any of the first and second supply channels. 3. The catalyst vessel according to claim 1 or 2 , wherein

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