JPH10245573A - Apparatus for removing carbon monoxide from reformed gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an apparatus for removing carbon monoxide from a reformed gas in a high removal rate of carbon monoxide at reduced consumption of hydrogen by reducing a feed of oxidizing air or oxygen necessary for the reaction. SOLUTION: A catalyst layer 14 and cooling layers 15 for cooling the layer 14 are laminated to form a plate, and the layer 14 is sandwiched between the layers 15. The layer 14 extends in the longer direction of a casing 11, and a catalyst 23 which can selectively oxidize carbon monoxide is packed into the middle of the width to form a catalyst packed zone 24. One side of the zone 24 serves as a gas inlet part 17, and the other side serves as a gas discharge part 18. A reformed gas FG and oxidizing air or oxygen change in direction from the longer direction to the rectangular direction and passes the zone 24. The catalyst 23 in the direction of flow of the gas is short and thin, and therefore has a less dispersed temperature distribution. Its entire surface can be uniformly cooled. As a consequence, the amount of oxidizing air or oxygen O2 used can be reduced.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a polymer electrolyte fuel cell power generation system by selectively removing carbon monoxide CO contained in a reformed gas obtained by reforming in a reformer. The present invention relates to a carbon monoxide removing device which is provided in the middle of a reformed gas supply line so as to be supplied to a fuel electrode of a battery.

[0002]

2. Description of the Related Art Among fuel cells, in the case of a polymer electrolyte fuel cell, methanol as a reforming material gas is reformed in a reformer, and then the reformed gas (fuel gas) is supplied to the fuel electrode of the fuel cell. However, if the reformed gas contains carbon monoxide (CO), the CO poisons the fuel cell electrode and deteriorates the performance. It is necessary to selectively remove CO in the reformed gas before supplying the reformed gas.

Conventionally, as a carbon monoxide removing device for removing CO in a reformed gas in order to satisfy such a need, a long cylindrical body 1 as shown in FIGS.
A plurality of small-diameter pipes 2 extending in parallel with the axial direction of the cylindrical body 1 are disposed in the inside of each of the pipes, and rhodium ( A cooling chamber 5 in which a catalyst 3 such as Rh) or ruthenium (Ru) is filled, and the outside of each tube 2 flows a cooling medium 4,
Oxidizing air or oxygen O ₂ is introduced together with the reformed gas FG from the inlet 2 a of each tube 2 opened at one end of the cylindrical body 1, and the cooling medium 4 is introduced into the cooling chamber 5 from the other end of the cylindrical body 1. To take out from the inlet 2a side of each pipe 2,
The reformed gas FG and the oxidized air or oxygen O ₂ are subjected to a reaction of CO + 1/2 O ₂ → CO ₂ by the catalyst 3 in each tube 2 so that CO in the reformed gas FG is selectively removed. As shown in FIG. 7, a ceramic catalyst carrier 6 having a large number of honeycomb-shaped passages 7 is placed in a casing 8 such that the passages 7 are parallel to the longitudinal direction of the casing 8. And the catalyst 3 capable of selectively oxidizing CO is supported in the form of a powder in the passage 7 of the catalyst carrier 6,
Oxidizing air or oxygen O ₂ is introduced together with the reformed gas FG from the inlet side of the casing 8 to cause a reaction for CO removal,
One in which the reformed gas from which CO is removed is supplied to the fuel electrode of the fuel cell, and the like.

[0004]

However, in the case of the carbon monoxide removing apparatus shown in FIG. 6, since the length of each of the pipes 2 arranged in parallel in the cylindrical body 1 is long, the apparatus does not have the same structure in the flow direction of the reformed gas. As the temperature difference of the catalyst 3 increases, a large temperature difference also occurs in the radial direction of the cylindrical body 1. Particularly, when there is a catalyst temperature difference in the flow direction of the reformed gas, the catalyst gas is introduced from the inlet 2 a of each pipe 2. Since the oxidized air or oxygen O ₂ does not uniformly react with carbon monoxide in the gas flow direction, a uniform reaction temperature cannot be achieved. As shown in FIG. 8 showing the relationship between the CO removal rate and the reaction temperature, CO and H when a rhodium (Rh) -based catalyst or a ruthenium (Ru) -based catalyst is used as a catalyst capable of selectively oxidizing CO are used. Looking at the removal rate of ₂ ,
In the case of using a Rh-based catalyst, as the reaction temperature increases as indicated by the symbol ◇, the removal rate of H ₂ is slightly increased, but the removal rate of CO is increased to 200 ° C. or higher as indicated by the mark ○. Then, there is a problem that the optimum temperature range is narrow because the temperature decreases, and when a Ru-based catalyst is used, even if the reaction temperature increases, the CO removal rate does not decrease as indicated by ●, but Δ When the H ₂ removal rate exceeds 100 ° C., the temperature rapidly increases, and in this case also, the range of the optimum temperature is narrow. When the side reaction (H ₂ +1/2 O ₂ → H ₂ O) that consumes hydrogen occurs, there is a problem that the amount of H ₂ as fuel to the fuel electrode of the fuel cell decreases, and as described above, for side reactions correspondingly much oxygen is employed when occurs, it is necessary to increase the introduced amount of the oxidizing air or oxygen O _2, usually in oxidizing atmospheric oxygen or oxygen theoretically required amount There is a problem that it is necessary to add about four times (oxidizing air stoichiometric ratio 4.0), and accordingly, the capacity of the compressor must be increased as a feeder. When the diameter of the tube 2 is large, a difference occurs in the catalyst temperature between the center and the periphery of the tube 2. On the other hand, when the diameter of the tube 2 is small, the pressure loss of the gas flow increases, It becomes difficult to pack the catalyst 3, and furthermore, the difference in pressure loss between the tubes 2 arranged in parallel. Flow distribution per al pipe 2 are different, there are problems such.

In the case of the carbon monoxide removing apparatus shown in FIG. 7, the reaction temperature becomes higher downstream in the same honeycomb-shaped passage. Therefore, when a heat exchanger is used for cooling, the honeycomb-shaped passage and the heat exchanger are used. Are arranged alternately, and there is a problem that the structure becomes complicated.

Therefore, the present invention provides a secondary reaction (H ₂ +1/2 O ₂ → H ₂ O) in which a hydrogen consumption reaction is performed when a main reaction for selectively removing carbon monoxide in a reformed gas is performed. ) To reduce the consumption of hydrogen,
The stoichiometric ratio is set to 4.0 by reducing the supply amount of the oxidizing air or oxygen.
It is intended to make it possible to make the reaction temperature of the catalyst-filled portion uniform.

[0007]

According to the present invention, in order to solve the above-mentioned problems, a catalyst layer and a cooling layer for adjusting a reaction temperature in the catalyst layer are horizontally provided inside a box-shaped casing. The catalyst layer is laminated so as to sandwich the catalyst layer with the cooling layer through the partition wall and CO 2
A catalyst for selectively oxidizing carbon monoxide is filled in the central portion of the catalyst layer of the CO removing portion so as to reduce the thickness and lengthen in the longitudinal direction of the casing. A catalyst-filled portion, one side of the width of the casing that is one side of the catalyst-filled portion is used as a portion for introducing reformed gas and oxidized air or oxygen, and the other side of the casing that is the opposite side of the catalyst-filled portion. As the outlet for the reformed gas and the oxidized air or oxygen, the reformed gas and the oxidized air or oxygen flow in the width direction of the casing. And a cooling medium introduction part and a discharge part of the cooling layer are respectively opened to the outside of the casing.

[0008] Since the reformed gas and oxidized air or oxygen flow through the introduction section in the longitudinal direction of the casing and then change the direction at right angles to pass through the catalyst filling section, the catalyst is short in the gas flow direction. Thus, the temperature difference between the catalysts is small, and since both surfaces of the catalyst-filled portion are cooled over the entire surface, uniform cooling can be performed. Further, since the catalyst is thin, the reaction temperature can be made uniform. Thereby, the supply amount of the oxidizing air or oxygen can be reduced, the stoichiometric ratio can be reduced, and the consumption of hydrogen in the reformed gas decreases.

A plurality of CO removing sections are formed by partitioning in the width direction in the casing, and the reforming gas and oxidizing air or oxygen introduction sections and discharge sections of each CO removal section are communicated with each other. In addition, when the inlet side and the outlet side of each cooling layer are connected to each other, carbon monoxide can be efficiently removed.

Further, if the catalyst filling section of the CO cooling section is divided by a large number of partition walls in the longitudinal direction of the casing, the catalyst can be packed as small blocks and the flow of reformed gas can be made uniform. it can.

[0011]

Embodiments of the present invention will be described below with reference to the drawings.

FIGS. 1A, 1B, and 1C show plate-type CO removing units 10a and 10b according to an embodiment of the present invention.
Are formed separately on the left and right inside one box-shaped casing 11, and the reformed gas FG introduced from one end side of the casing 11
And oxidizing air or oxygen O ₂ simultaneously in two CO removing units 1
0a and 10b and carbon monoxide CO in the reformed gas FG
Are shown below.

More specifically, a casing 1 formed in a box shape
1, a central partition wall 12 is provided at a central portion to partition left and right, and horizontal partition walls 13 are arranged in multiple stages symmetrically with respect to the central partition wall 12 so as to sandwich catalyst every other one inside. The catalyst layer 14 is formed by laminating a plate-type catalyst layer 14 for filling the catalyst layer and a plate-type cooling layer 15 for flowing a cooling medium to adjust the reaction temperature in the catalyst layer 14. Are sandwiched between the cooling layers 15 from both sides, and partition walls 16 extending in the left-right direction only at the respective center portions of the catalyst layers 14 and the cooling layer 15 are arranged at required intervals to form a large number of small spaces. Further, one side of the small space forming portion at the center of the catalyst layer 14 is defined as a gas introduction portion 17 along the longitudinal direction of the casing 11, and the other side is defined as a gas outlet portion 18. One side of the small space forming part is a cooling medium introduction part 1 And then, the opposite side cooling medium outlet section 2
At one end of the casing 11 which is the inlet side of the gas and the cooling medium, the closing plate 21 is left, leaving only the gas introduction part 17 of each catalyst layer 14 and the cooling medium introduction part 19 of each cooling layer 15. On the other side of the casing 11, except for the gas introduction section 17 of each catalyst layer 14 and the cooling medium introduction section 19 of each cooling layer 15, the casing 11 is closed with the closing plate 22, and the catalyst layer 14 is adjacent to the catalyst layer 14. In each small space formed between the partition walls 16 or between the partition walls 16 at both ends and the closing plates 21 and 22, a catalyst 23 capable of selectively oxidizing carbon monoxide is packed with a reduced thickness. By forming the catalyst filling section 24, the left and right separate CO removing sections 10a and 10b are configured.

Reference numeral 25 denotes a perforated plate provided on the side of the gas introduction section 17 of the catalyst filling section 24 for adjusting the flow rate of gas. Reference numeral 26 denotes a catalyst layer for uniformly flowing oxidized air or oxygen O ₂ into each small space. 14 is a perforated plate for adjusting the flow rate provided in the gas introduction portion 17 of the fuel cell 14, and a casing 11 is provided in a flow path 27 formed between the perforated plate 26 and the inner wall or the central partition wall 12 of the casing 11.
Oxidizing air or oxygen O ₂ can be supplied from the outside. Reference numeral 28 denotes a reformed gas inlet provided in the casing 11 corresponding to each catalyst layer 14 so as to guide the reformed gas FG to the gas introduction unit 17 of each catalyst layer 14 of the two CO removing units 10a and 10b. 29 is a reformed gas outlet provided on the opposite side of the casing 11 corresponding to each catalyst layer 14, 30 is a cooling medium inlet provided on one end side of the casing 11 for introducing the cooling medium 4 into each cooling layer 15, Reference numeral 31 denotes a cooling medium outlet provided on the opposite side of the casing 11.

The cooling medium 4 is shown in FIG.
The flow direction may be reversed, and the cooling medium may be introduced from the cooling medium outlet 31 and discharged from the cooling medium inlet 30. Although the case where 10a and 10b are configured is shown, a configuration in which one CO removing unit is configured in the casing 11 may be used.

Therefore, the reformed gas FG is
When the reformed gas FG is introduced from the first inlet 28, the reformed gas FG enters the catalyst filling section 24 from the gas introduction section 17 of the catalyst layer 14 of each layer in the casing 11 through the flow control porous plate 25.
On the other hand, the oxidized air or oxygen O ₂ is guided from the outside of the casing 11 to the flow path 27, passes through the perforated flow control plate 26 partitioning the flow path 27, and uniformly fills the catalyst with the reformed gas FG. In the part 24, the main reaction (CO + 1/2 O ₂ → CO ₂ ) is performed in the presence of the catalyst 23. During this time, since the cooling medium 4 is flowing through the cooling layer 15,
A cooling action can be performed when removing carbon monoxide by the exothermic reaction.

In the above, according to the present invention, as described above, the catalyst 23 is filled in the central portion in the width direction of the reaction portion of the plate-type catalyst layer 14 formed so as to be longer in the longitudinal direction of the casing 11. As the charging section 24, the reformed gas FG and the oxidized air or oxygen O ₂ flow in a direction perpendicular to the longitudinal direction of the casing 11 and pass through the catalyst charging section 24. It is divided into small sections by a large number of partition walls 16, and the catalyst filling section 2
The catalyst 23 of No. 4 has a small thickness and is short in the gas flow direction, and the gas flows uniformly throughout the catalyst filling portion 24, and the catalyst filling portion 24 is sandwiched between the cooling layers 15 from both sides. The uniform cooling is performed over the entire surface, so the temperature difference in the gas flow direction and thickness direction is small, and the cooling area can be made larger than in the case of a circular tube, so that the entire catalyst is cooled uniformly. It can be performed. Thus, it is possible to equalize the reaction temperature in the catalyst packed portion 24, it is possible to maintain the reaction temperature optimum value is high and H is low ₂ removal rate removal rate of CO shown in FIG. 8, CO + 1 / 2 O ₂ → H ₂ +1/2 O ₂ → H ₂ O which occurs in addition to the main reaction of CO ₂ or CO + 3H ₂ → CH ₄ + H
Side reactions such as ₂ O are reduced, and accordingly, the supply amount of oxidizing air or oxygen O ₂ can be reduced in advance. As a result, the oxidizing air stoichiometric ratio is set at 4.0 as described above. , The stoichiometric ratio of oxidizing air can be 4.0 or less.

2 and 3 show the relationship between the stoichiometric ratio of oxidizing air and the outlet CO concentration and the relationship between the stoichiometric ratio of oxidizing air and the hydrogen concentration. Although the CO concentration at the outlet of the carbon monoxide removal device is low as indicated by the symbol △ in FIG. 2, a side reaction occurs and the hydrogen concentration at the outlet of the carbon monoxide removal device is also reduced as indicated by the symbol ▽ in FIG. It is in.

In the present invention, since the configuration is as described above, the supply amount of the oxidizing air or oxygen O ₂ can be reduced. Therefore, the CO concentration at the outlet of the carbon monoxide removing device in FIG. A sufficient CO removal effect can be obtained even if the oxidizing air stoichiometric ratio is made lower than 4.0 by shifting to the upper left, and at the same time, the hydrogen concentration at the outlet is reduced by the hydrogen concentration at the inlet of the carbon monoxide removal device shown by the broken line in FIG. The hydrogen consumption can be reduced with almost no change from the concentration a. Accordingly, the efficiency of the fuel cell can be improved.

The apparatus for removing carbon monoxide of the present invention is used, for example, in a fuel cell power generator for ship propulsion.

FIG. 4 shows a power generator using a polymer electrolyte fuel cell as a fuel cell for ship propulsion. The carbon monoxide removing apparatus I of the present invention is reformed by
It is installed and used downstream of the CO converter 33 so as to remove CO in the reformed gas passing through the converter 33.

The solid polymer electrolyte fuel cell power generator will be described. A cell in which a solid polymer electrolyte membrane 34 is sandwiched between both electrodes of an oxygen electrode (cathode) 35 and a fuel electrode (anode) 36 via a separator. A reformer 32 is installed outside a solid polymer electrolyte fuel cell FC which is stacked and has a cooling unit 37 in an arbitrary cell and is a stack, and methanol as a fuel is stored in a methanol tank 38.
, Pressurized by a methanol pump 39, and supplied to a reforming chamber of a reformer 32 via an evaporator 40 and a preheater 41,
The gas (fuel gas) FG reformed by the reformer 32 passes through the preheater 41, the CO converter 33, and the heat exchanger 42, and then CO is removed by the carbon monoxide removing device I of the present invention. Thereafter, the temperature is lowered to 100 ° C. or lower through a heat exchanger 43, further, through a reformed gas reservoir 44, through a humidifier 45, and the fuel electrode 3.
The anode exhaust gas AG discharged from the fuel electrode 36 is supplied to the combustion chamber of the reformer 32 through the anode exhaust gas line 47 and burned after the moisture is removed by the steam separator 46. At the same time, a part of the anode exhaust gas AG is bypassed by a bypass line 48 branched from the anode exhaust gas line 47 and introduced into the catalytic combustor 49. Control valves 50 and 51 are provided, and a control unit 53 that controls the flow rate control valves 50 and 51 so as to adjust the anode exhaust gas flow rate in accordance with the temperature detected by the thermometer 52 that detects the temperature of the combustion chamber of the reformer 32 is provided. It is a configuration provided. Further, the catalytic combustor 49 is configured to introduce the combustion gas discharged from the reformer 32 through a combustion gas line and a part of the air compressed by a compressor 55 driven by an exhaust gas turbine 54. Is introduced to burn unreacted components in the anode exhaust gas, and when the amount of anode exhaust gas from the bypass line 48 entering the catalytic combustor 49 is small,
A part of methanol is pressurized by the pump 56 from the methanol tank 38 and introduced into the catalytic combustor 49 for combustion.

Reference numeral 57 denotes a steam generator; 58, a steam line;
Reference numeral 9 denotes a supply line for supplying air A as an oxidant gas OG to the oxygen electrode 35, and reference numerals 60 and 61 denote heat exchange lines provided for supplying a cathode exhaust gas CG discharged from the oxygen electrode 35 to a combustion chamber of the reformer 32. And steam-water separator.

When the carbon monoxide removing device I of the present invention is used in such a polymer electrolyte fuel cell power generator, the reformer 3
2 and CO converter 33 are both plate type,
It can be laminated in combination with the carbon monoxide removing device I of the present invention.

FIG. 5 shows, as an example, a case where the carbon monoxide removing apparatus I of the present invention is superposed on a CO converter 33 and a reformer 32. A plate-type reforming chamber 63 filled with a reforming catalyst 62 in a portion thereof and a combustion chamber 65 filled with a combustion catalyst 64 are divided into partition walls 6.
The reforming chamber 63 is sandwiched between the combustion chambers 65. The reforming chamber 63 is supplied from the inlet side with a reforming raw material (methanol) and a steam 67 supply line. A combustion gas 68 is supplied from a supply line from an inlet side, burned in a combustion chamber 65, and heat generated by the combustion is absorbed in a reforming chamber 63 through a partition wall 66 to cause a reforming reaction to be performed. The exhaust gas is discharged to the reformed gas line 69 on the outlet side of the reforming chamber 63, and the combustion exhaust gas is discharged from the outlet side of the combustion chamber 65. CO converter 33
Is formed by stacking a plate-type shift chamber 71 filled with a catalyst 70 on both sides of a plate-type cooling chamber 73 via a partition wall 72, and reforming gas F reformed in a reformer 32.
G is converted in the conversion chamber 71 of the CO converter 33 and discharged.

The above three devices are stacked in a plate type, the outlet side of the reformer 32 and the inlet side of the CO converter 33 are connected by a reformed gas line 69, and each cooling chamber 7 is connected.
3 is supplied with a cooling medium from a cooling medium supply line 74, and the reformed gas discharged from the shift chamber 71 of the CO converter 33 is passed through a reformed gas line 69 of the carbon monoxide removal device I of the present invention. It is introduced into the catalyst layer 14.

FIG. 5 is an example, and the reformer 32 and C
The combination method is arbitrary, such as exchanging the O converter 33.

As described above, the carbon monoxide removing apparatus I of the present invention is laminated and integrated with the plate-type reformer 32 and the plate-type CO converter 33, thereby achieving compactness and power generation. The system configuration of the device can be simplified.

The catalyst filling section 24 may be formed in a honeycomb shape to support the catalyst 23. In the case of a honeycomb catalyst, the partition wall 16 can be eliminated because the catalyst does not easily move due to vibration or the like.

[0030]

EXAMPLES The results of experiments conducted by the present inventors will be described.

In the apparatus for removing carbon monoxide in a 10 kW class methanol reformed gas, the reformed gas flow rate is 0.458 kmol / H (10.25 Nm
³ / H) Catalyst volume: 430 cm ³ Heat value (stoichiometric ratio 4): 868 Kcal / H Oxidized air amount (stoichiometric ratio 4): 11.4 Nl / min. 100m diameter
m, when the length of each tube 2 is 1500 mm, the catalyst temperature difference is about 50 ° C. in the gas flow direction and about 5 ° in the radial direction.
At 0 ° C., the part where the cooling medium is put is cooled much.

On the other hand, in the case of the present invention, the catalyst layer 14
The flow rate Q and the temperature rise when using water and air as the cooling medium are 450 mm, the length is 600 mm, and the height is 15 mm. Difference) When ΔT was determined, in the case of water cooling: Q = 1.44 l / min ΔT = 10 ° C.
(When the stoichiometric ratio is 4.0) In the case of air cooling: Q = 960 Nl / min ΔT = 60 ° C.
(At a stoichiometric ratio of 4.0). In the case of air cooling, since ΔT is large, it is necessary to reduce the oxidizing air stoichiometric ratio to 4.0 or less in order to reduce ΔT. Since ΔT is 10 ° C. in the case of water cooling, the catalytic reaction temperature can be maintained at the optimum temperature where the CO removal rate is high and the hydrogen removal rate is low in FIG.

[0033]

As described above, according to the apparatus for removing carbon monoxide in reformed gas of the present invention, a catalyst capable of selectively removing carbon monoxide is provided in a plate-type catalyst layer by reducing the thickness. The length of the catalyst is shortened in the direction in which the reformed gas and the oxidizing air or oxygen flow, and the catalyst layer is laminated and sandwiched from both sides by a plate-type cooling layer. When CO is removed by an exothermic reaction when passing through the catalyst, cooling is performed by the cooling medium flowing through the cooling layer, so that the temperature difference of the catalyst is extremely small, and the catalyst filling portion uniformly cools the whole. The reaction temperature can be made uniform, the supply amount of oxidizing air or oxygen can be reduced, and the stoichiometric ratio can be reduced as compared with the conventional method. Hydrogen consumption As a result, the efficiency of the fuel cell can be improved, the temperature distribution can be made uniform, the stability of the reaction can be improved, and the supply power of the compressor can be reduced by reducing the supply of oxidized air. Can be greatly reduced, and the like. Furthermore, the plate-type carbon monoxide removal device of the present invention is laminated with a plate-type reformer and a plate-type CO converter. By integrating them, an excellent effect that the power generation device can be made compact can be obtained.

[Brief description of the drawings]

FIG. 1 shows an embodiment of a carbon monoxide removing apparatus according to the present invention, in which (a) is a cut side view, and (b) is X in (a).
FIG. 3C is a view as seen in the direction of the arrow X, and FIG. 3C is a view as viewed in the direction of the arrow YY in FIG.

FIG. 2 Stoichiometric ratio of oxidizing air and CO at the outlet of carbon monoxide removing device
It is a figure which shows the relationship of density.

FIG. 3 is a graph showing the relationship between the stoichiometric ratio of oxidizing air and the concentration of hydrogen at the outlet of the carbon monoxide removing device.

FIG. 4 is a system diagram showing an example of a polymer electrolyte fuel cell power generator.

FIG. 5 is a schematic diagram showing a case where the carbon monoxide removing device of the present invention is laminated with a plate-type reformer and a CO converter to be integrated.

FIG. 6 shows an example of a conventional carbon monoxide removing apparatus, in which (A) is a cut side view, and (B) is a view taken along the line ZZ of (A).

FIG. 7 is a sectional view showing another example of the conventional carbon monoxide removing device.

FIG. 8 is a diagram showing the relationship between the reaction temperature of the catalyst and the removal rates of CO and H ₂ .

[Explanation of symbols]

Reference Signs List 4 cooling medium 10a, 10b CO removal unit 11 casing 12 central partition wall 13 partition wall 14 catalyst layer 15 cooling layer 16 partition wall 17 gas introduction unit 18 gas extraction unit 19 cooling medium introduction unit 20 cooling medium extraction unit 23 catalyst 24 catalyst filling unit 32 reformer 33 CO converter 63 reforming chamber 65 combustion chamber 71 shift chamber FG reformed gas O ₂ oxidized air or oxygen

Claims (5)

[Claims] 1. A catalyst layer and a cooling layer for adjusting a reaction temperature in the catalyst layer are stacked inside a box-shaped casing so as to sandwich the catalyst layer between the cooling layers via a horizontal partition.
A catalyst for selectively oxidizing carbon monoxide is filled in the central portion of the catalyst layer of the CO removing portion so as to reduce the thickness and lengthen in the longitudinal direction of the casing. A catalyst-filled portion, one side of the width of the casing that is one side of the catalyst-filled portion is used as a portion for introducing reformed gas and oxidized air or oxygen, and the other side of the casing that is the opposite side of the catalyst-filled portion. As the outlet for the reformed gas and the oxidized air or oxygen, the reformed gas and the oxidized air or oxygen flow in the width direction of the casing. An opening and an outlet for the cooling medium and an inlet and an outlet for the cooling medium of the cooling layer are respectively opened to the outside of the casing. 2. A plurality of CO removing sections are formed by partitioning in the width direction in the casing, and the reforming gas and oxidizing air or oxygen introduction sections and discharge sections of each CO removal section are communicated with each other, 2. The apparatus for removing carbon monoxide in a reformed gas according to claim 1, wherein an inlet side and an outlet side of each cooling layer communicate with each other. 3. The apparatus for removing carbon monoxide in a reformed gas according to claim 1, wherein the catalyst filling section of the CO cooling section is partitioned by a number of partition walls in the longitudinal direction of the casing. 4. The apparatus for removing carbon monoxide in a reformed gas according to claim 1, wherein the catalyst layer and the cooling layer of the CO removing section are formed in a plurality of layers. 5. The apparatus for removing carbon monoxide in reformed gas according to claim 1, wherein the reformer and the CO converter are of a plate type, and are integrated with the plate type reformer and the CO converter.