JP2018114432A - Reactor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a reactor capable of maintaining an isothermal environment with high heat transfer efficiency while suppressing stress loss of a raw material gas distributed in a reaction gas tube.SOLUTION: There is provided a reactor for conducting an exothermic reaction and an endothermic reaction, having a plurality of first flow passages 4a and 4b, a confluent flow passage 4d at which the plurality of first flow passages 4a and 4b are merged, and a second flow passage 4c connected to the confluent flow passage 4d, a reaction flow passage 4 in which a raw material gas flows in a direction from the plurality of first flow passages 4a and 4b to the second flow passage 4c, and a medium flow passage 3 in which a temperature adjustment medium for adjusting a temperature of the reaction flow passage 4 flows, and the reaction flow passage 4 is arranged in the medium flow passage 3.SELECTED DRAWING: Figure 2

Description

  The present invention relates to a reaction apparatus.

  Conventionally, a reaction apparatus that generates methane gas from a raw material gas by methanation reaction is known (see, for example, Patent Document 1). In recent years, in order to effectively perform the methanation reaction, a multi-tubular (shell tube) reactor that removes heat of reaction has also been proposed.

U.S. Pat. No. 3,933,446

  In a general multitubular reactor, when the tube diameter (inner diameter) of the reaction gas pipe is set large, if a large exothermic reaction occurs, a difference in temperature distribution in the cross-sectional direction of the reaction gas pipe tends to occur. For this reason, there has been a problem that catalyst deterioration such as sintering and coking easily occurs. On the other hand, when the tube diameter (inner diameter) is set small and the number of reaction gas pipes is increased, a preferable isothermal environment is obtained because there is almost no difference in temperature distribution, but the pressure loss in the reaction gas pipe increases. There is a problem that it is difficult to efficiently flow more source gas into the reaction gas pipe.

  The present invention has been made in view of the above-described circumstances, and provides a reaction apparatus capable of maintaining an isothermal environment with high heat transfer efficiency while suppressing the pressure loss of the raw material gas flowing through the reaction gas pipe. It is intended.

  In order to achieve the above object, in the present invention, as a first solving means related to a reaction apparatus, a reaction apparatus that performs an exothermic reaction or an endothermic reaction, the plurality of first flow paths, and the plurality of first flows. Reaction in which source gas flows in a direction from the plurality of first flow paths toward the second flow path, having a merge flow path where the paths merge and a second flow path connected to the merge flow path A flow path and a medium flow path through which a temperature adjusting medium for adjusting the temperature inside the reaction flow path is provided, the reaction flow path is provided inside the medium flow path, and the plurality of first flows You may employ | adopt the means that each cross-sectional area of a path is smaller than the cross-sectional area of the said 2nd flow path.

  In the present invention, as the second solving means relating to the reaction apparatus, in the first solving means, a catalyst is provided inside the plurality of first flow paths and the second flow paths, and the catalyst May adopt a means of promoting generation of the target gas from the source gas.

  In the present invention, as a third solving means relating to the reaction apparatus, in the first or second solving means, the medium flow path in which the temperature control medium flows in positions corresponding to the plurality of first flow paths. Means may be adopted in which the first cross-sectional area is larger than the second cross-sectional area of the medium flow path through which the temperature control medium flows at a position corresponding to the second flow path.

  In the present invention, as a fourth solving means related to the reaction apparatus, in any one of the first to third solving means, the medium flow path is a first flow in which the temperature adjusting medium flows into the medium flow path. You may employ | adopt the means of having an inlet_port | entrance and a 2nd inlet_port | entrance, and an outlet port from which the said temperature control medium flows out from the said medium flow path.

  In the present invention, as a fifth solving means relating to the reaction apparatus, in any one of the first to third solving means, the medium flow path includes an inlet through which the temperature adjusting medium flows into the medium flow path. A means of having a first outlet and a second outlet from which the temperature control medium flows out from the medium flow path may be adopted.

  In the present invention, as a sixth solving means relating to the reaction apparatus, in any one of the first to third solving means, the medium flow path includes an inlet through which the temperature adjusting medium flows into the medium flow path. The temperature adjusting medium flowing out from the medium flow path, the flow direction of the source gas in the reaction flow path, and the temperature adjusting medium flowing from the inlet toward the outlet You may employ | adopt the means that it is the same as a flow direction.

  In the present invention, as a seventh solving means relating to the reaction apparatus, in any one of the first to third solving means, the medium flow path includes an inlet through which the temperature adjusting medium flows into the medium flow path. The temperature adjusting medium flowing out from the medium flow path, the flow direction of the source gas in the reaction flow path, and the temperature adjusting medium flowing from the inlet toward the outlet You may employ | adopt the means that it is contrary to a flow direction.

  According to the present invention, in a reaction apparatus that performs an exothermic reaction or an endothermic reaction, when the source gas flows in the reaction channel, the source gas passes through the first channels having a smaller cross-sectional area than the second channel. Since it flows and then merges in the merging channel and flows in the second channel, an isothermal environment can be maintained while reducing the overall pressure loss of the reaction channel.

It is a block diagram which shows the whole structure of the reaction apparatus which concerns on one Embodiment of this invention. It is sectional drawing which shows the principal part of the reactor main body with which the reaction apparatus which concerns on one Embodiment of this invention is equipped, Comprising: (a) is a figure which shows a reactor main body, (b) is the reactor which concerns on the modification 1. It is a figure which shows a main body. It is sectional drawing which shows the principal part of the reactor main body with which the reaction apparatus which concerns on one Embodiment of this invention is equipped, Comprising: (a) is a figure which shows the reactor main body which concerns on the modification 2, (b) is a modification. 3 is a view showing a reactor main body according to FIG.

  Hereinafter, a reaction apparatus according to an embodiment of the present invention will be described with reference to the drawings. In the following drawings, the scale of each member is appropriately changed in order to make each member a recognizable size.

As shown in FIG. 1, a reaction apparatus A according to an embodiment includes a reactor main body 1 (reactor main bodies 1A, 1B, 1C, and 1D described later) and a refrigerant supply device 2.
The reactor main body 1 is a reactor that generates a methane-containing gas (target gas) by subjecting a raw material gas to a chemical reaction (methanation reaction) in the presence of a catalyst. As will be described later, the reactor main body 1 includes a reaction flow path 4 having a reaction field filled with a catalyst (methanation catalyst), and supplies a raw material gas to the reaction flow path 4. In the reactor main body 1, the reaction channel 4 is cooled by the refrigerant supplied from the refrigerant supply device 2 as a temperature control medium.

  The refrigerant supply device 2 is a device that supplies a predetermined specification (refrigerant specification) refrigerant (temperature control medium) to the reactor main body 1 so that the reactor main body 1 is an isothermal reactor. The refrigerant supply device 2 supplies a refrigerant to a medium flow path 3 to be described later, recovers the heated refrigerant (return refrigerant) used for cooling the reaction field (catalyst filling region) from the reactor body 1 and recycles it. It is a circulating refrigerant supply device that cools and supplies the reactor main body 1 as the refrigerant having the predetermined specifications.

Here, the raw material gas supplied to the reactor main body 1 is, for example, a mixed gas in which carbon monoxide (CO) and hydrogen (H ₂ ) are mixed at a predetermined ratio (molar ratio). Such a raw material gas becomes methane (CH ₄ ) and water (H ₂ O) by a methanation reaction (exothermic reaction) in the presence of a catalyst, as shown in the following reaction formula. That is, the methane-containing gas is a mixed gas composed of methane (CH ₄ ) and water vapor (H ₂ O).
CO + 3H ₂ = CH ₄ + H ₂ O + 206 (kJ / mol)

  Such methanation reaction occurs based on the principle of thermodynamic equilibrium, and the reaction rate depends on the pressure and temperature of the reaction field and affects the rate of methane production. Therefore, it is necessary to control the temperature of the reaction field in order to efficiently advance the methanation reaction under a specific pressure. Further, in order to bring the methanation reaction close to the maximum efficiency (ideal state), it is necessary to maintain the entire region of the reaction field, more specifically, the entire region of the catalyst forming the reaction field at the optimum temperature. For example, when the pressure in the reaction field is normal pressure, the optimum temperature is in the range of 300 to 400 ° C. Under such circumstances, the reactor main body 1 needs to be configured as an isothermal reactor.

  Further, in order to take away a large amount of heat such as 206 (kJ / mol) shown in the above reaction formula from the reaction channel 4, it is necessary to efficiently transfer the heat generated by the methanation reaction from the reaction channel 4 to the refrigerant. is there. For this reason, it is necessary to increase the heat transfer area for the refrigerant by setting the diameter of the reaction channel 4 per one small and increasing the number of the reaction channels 4.

Generally, when the diameter of the reaction channel 4 is reduced, the pressure loss in the reaction channel 4 increases, and the source gas hardly flows in the reaction channel 4.
For example, the Cozeny Kalman equation is known as a calculation formula for pressure loss in a packed bed in which particles or the like are filled in a flow path. Based on this equation, the pressure loss ΔP in the flow path is obtained by calculating the length L of the flow path, the superficial velocity of the gas (the speed of the gas assuming no packed bed) v, and (1-ε) / It is proportional to ε ³ (where ε is a space factor). For this reason, as the inner diameter of the reaction channel 4 is reduced, the pressure loss increases, and the source gas hardly flows in the reaction channel 4.
In the present embodiment, in consideration of efficient heat transfer from the reaction channel 4 to the refrigerant, the pressure loss allowable in the reaction channel 4 is practically about 100 kPa.

  Next, with reference to FIG.2 and FIG.3, the reactor main body 1 with which the reaction apparatus A is provided is demonstrated concretely. In FIG.2 and FIG.3, the same code | symbol is attached | subjected to the same member which comprises the reactor main body 1 which concerns on embodiment and modification of this invention, The description is abbreviate | omitted or simplified.

(Reactor body 1 according to this embodiment)
Fig.2 (a) is sectional drawing which shows the principal part of reactor main body 1A (1) with which the reaction apparatus A which concerns on one Embodiment of this invention is provided.
The reactor main body 1 </ b> A includes a reaction channel 4 and a medium channel 3.
The reaction channel 4 is connected to two first channels 4a and 4b (a plurality of first channels), a merge channel 4d where the first channels 4a and 4b merge, and a merge channel 4d. A second flow path 4c. Each of the first flow paths 4a and 4b and the second flow path 4c is formed in a cylindrical shape (straight tube), for example. The raw material gas supplied to the reactor main body 1A shown in FIG. 1 is supplied to the first flow paths 4a and 4b, and the raw material gas flowing through the first flow paths 4a and 4b merges in the merging flow path 4d. The two flow paths 4c are circulated. That is, the source gas flows in the direction from the first flow paths 4a and 4b toward the second flow path 4c. A catalyst 5 is provided inside the first flow paths 4 a and 4 b and the second flow path 4 c, and the catalyst 5 promotes the generation of the target gas from the raw material gas flowing through the reaction flow path 4.

  The medium flow path 3 is provided around the reaction flow path 4. In other words, the reaction channel 4 is provided inside the medium channel 3. The medium flow path 3 includes an inlet 3a through which the refrigerant flows into the medium flow path 3 and an outlet 3b through which the refrigerant flows out of the medium flow path 3, and is formed in a cylindrical shape (straight tube), for example. . A refrigerant for setting the atmosphere temperature of the catalyst to an isothermal atmosphere, that is, a refrigerant for adjusting the temperature of the reaction flow path 4 flows in the internal space of the medium flow path 3. The flow direction D1 of the raw material gas in the reaction channel 4 is opposite to the flow direction D2 of the refrigerant flowing from the inlet 3a toward the outlet 3b (opposite flow).

  In the structure shown in FIG. 2A, the cross-sectional area of each of the first flow paths 4a and 4b is smaller than the cross-sectional area of the second flow path 4c. For example, the inner diameter P of each of the first flow paths 4a and 4b is 4 (mm). The inner diameter Q of the second flow path 4c is 8 (mm). Moreover, the length L1 of each catalyst filling part of the first flow paths 4a and 4b is 0.5 (m). The length L2 of the catalyst filling portion of the second flow path 4c is 0.5 (m).

In each of the first flow paths 4a and 4b, the cross-sectional area is 12.57 (mm ² ), the volume is 1.26 × 10 ⁻⁵ (m ³ ), and the outer surface area is 2.51 × 10 ⁻² ( mm ² ). The gas linear velocity (350 ° C.) is 6.339 (m / sec).
The volume V of the catalyst 5 provided in each of the first flow paths 4a and 4b is 1.26 × 10 ⁻⁵ (m ³ ), and the heat transfer area A is 0.01257 (m ² ). For this reason, the heat transfer efficiency, that is, the value (A / V) obtained by dividing the heat transfer area A by the catalyst volume V is about 1000 (1 / m).
When the pressure loss in the first flow paths 4a and 4b is calculated using the Cozeny Kalman equation, the pressure loss ΔP is about 50.7 kPa. Here, the calculation conditions are as follows: catalyst particle diameter Dp is 1.0 (mm), gas flow rate is 3.5 × 10 ⁻⁵ (m ³ / sec), constant k is 180, gas viscosity μPas is 30 (H ₂ is 75% and CO is 25%), Φs is 1.0, and the filling rate ε is 0.6.

In the second flow path 4c, the cross-sectional area is 50.27 (mm ² ), the volume is 5.03 × 10 ⁻⁵ (m ³ ), and the outer surface area is 5.03 × 10 ⁻² (mm ² ). is there. The gas linear velocity (350 ° C.) is 1.585 (m / sec).
The volume V of the catalyst 5 provided in the second flow path 4c is 5.03 × 10 ⁻⁵ (m ³ ), and the heat transfer area A is 0.02513 (m ² ). For this reason, the heat transfer efficiency, that is, the value (A / V) obtained by dividing the heat transfer area A by the catalyst volume V is about 500 (1 / m).
When the pressure loss in the second flow path 4c is calculated using the Cozeny Kalman equation, the pressure loss ΔP is about 12.7 kPa. Here, the calculation conditions are the same as in the case of the first flow paths 4a and 4b.

  In the reactor main body 1A configured as described above, the raw material gas flows in the direction indicated by the flow direction D1 through the inlets (the upper ends shown in FIG. 2A) of the first flow paths 4a and 4b. 4 is continuously supplied. First, in each reaction field of the first flow paths 4a and 4b, a methanation reaction based on the action of the catalyst 5 occurs, and a part of the raw material gas is converted into a methane-containing gas (target gas). Thereafter, the methane-containing gas and the raw material gas that has not been converted to the methane-containing gas in the first flow paths 4a and 4b flow out of the first flow paths 4a and 4b, merge in the merge flow path 4d, and then the second flow It is supplied to the path 4c.

  In the reaction field of the second flow path 4c, a methanation reaction based on the action of the catalyst 5 occurs, and the remaining raw material gas is converted into a methane-containing gas. Thereafter, the methane-containing gas generated in the first flow paths 4a and 4b and the second flow path 4c is discharged from the outlet (the lower end shown in FIG. 2A) of the second flow path 4c in the direction indicated by the flow direction D1. That is, it flows out from the reaction channel 4.

  Such methanation reaction is an exothermic reaction as described above, and the first flow paths 4a and 4b and the second flow path 4c in which the catalyst 5 is provided release heat. In the reactor main body 1 having the medium flow path 3, the reaction field is cooled by removing heat of the reaction field formed in the reaction flow path 4 by the refrigerant flowing through the medium flow path 3 by heat exchange.

  Furthermore, since the pressure loss ΔP in the first flow paths 4a and 4b is about 50.7 kPa and the pressure loss ΔP in the second flow path 4c is about 12.7 kPa, the total pressure loss in the reaction flow path 4 is 63.4 kPa. The heat transfer efficiency (A / V) in the first flow paths 4a and 4b is about 1000 (1 / m), and the heat transfer efficiency (A / V) in the second flow path 4c is about 500 (1 / m). Therefore, the average A / V in the reaction channel 4 is about 750 (1 / m).

According to the present embodiment, when the merged flow path 4d is provided between the plurality of first flow paths 4a and 4b and the second flow path 4c, the reaction flow path 4 is configured by only one. As a result, the length L2 of the second flow path 4c is shortened, and the overall pressure loss of the reaction flow path 4 can be reduced. Further, in the first flow paths 4a and 4b, a methanation reaction with high heat transfer efficiency can be performed.
In particular, it is possible to reduce the overall pressure loss in the reaction channel 4 from 100 kPa, which is a practically allowable pressure loss, and to maintain an isothermal environment with high heat transfer efficiency.

  In particular, in the direction indicated by the flow direction D1 of the raw material gas, the methanation reaction occurs from a position close to the inlet of the reaction flow path 4, so that mainly the amount of heat generated in the first flow paths 4a and 4b increases. On the other hand, in the second flow path 4c, the methanation reaction of most of the raw material gases has been completed, so the amount of heat generated in the second flow path 4c is small. For this reason, the methanation reaction can be efficiently performed in the first flow paths 4a and 4b having higher heat transfer efficiency than the second flow path 4c.

  In the reaction channel 4 having the above structure, the reaction rate of the methanation reaction in each of the first channels 4a and 4b is 33%, that is, a total reaction rate of 66% is obtained in the first channels 4a and 4b. it is conceivable that. Moreover, it is considered that the reaction rate of the methanation reaction in the second flow path 4c is 33%. Depending on the reaction rate of the methanation reaction in each of the first flow paths 4a and 4b and the second flow path 4c, the lengths and inner diameters of the first flow paths 4a and 4b and the second flow path 4c may be adjusted as appropriate. .

(Modification 1 of reactor body 1)
FIG.2 (b) is sectional drawing which shows the principal part of reactor main body 1B (1) which concerns on the modification 1 of one Embodiment of this invention.
The reactor main body 1B is different from the reactor main body 1A described above in terms of the shape of the medium flow path 3. The medium flow path 3 of the reactor main body 1B includes a first inlet 3a1 and a second inlet 3a2 into which the refrigerant flows into the medium flow path 3, and an outlet 3b from which the refrigerant flows out of the medium flow path 3. A refrigerant having a flow rate F1 (m ³ / sec) is supplied from the first inlet 3a1 toward the inside of the medium flow path 3 (flow direction D2). A refrigerant having a flow rate F2 (m ³ / sec) is supplied from the second inlet 3a2 toward the inside of the medium flow path 3 (flow direction D3).

Further, the first cross-sectional area S1 of the medium flow path 3 through which the refrigerant flows at the position corresponding to the first flow paths 4a and 4b is the medium flow path through which the refrigerant flows at the position corresponding to the second flow path. It is larger than the second cross-sectional area S2.
In this case, the refrigerant flow rate U1 (m / sec) in the first cross-sectional area S1 is U1 = (F1 + F2) / S1. Moreover, the flow velocity U2 (m / sec) of the refrigerant in the second cross-sectional area S2 is U2 = F1 / S2.

  The “first cross-sectional area S1 through which the refrigerant flows” is obtained by subtracting the cross-sectional area of the first flow paths 4a and 4b from the cross-sectional area of the medium flow path 3 where the first flow paths 4a and 4b are not provided. It means an area, and means an area where the refrigerant flowing around the first flow paths 4 a and 4 b can flow in the medium flow path 3. Similarly, “second cross-sectional area S2 through which the refrigerant flows” means an area obtained by subtracting the cross-sectional area of the second flow path 4c from the cross-sectional area of the medium flow path 3 in which the second flow path 4c is not provided. In the medium flow path 3, it means an area through which the refrigerant flowing around the second flow path 4c can flow.

  As described above, since the methanation reaction occurs from a position close to the inlet of the reaction flow path 4, the amount of heat generated in the first flow paths 4a and 4b increases, and in the second flow path 4c, most of the source gas meta- Since the nation reaction has ended, the amount of heat generated in the second flow path 4c is small. For this reason, in order to perform the methanation reaction more efficiently, it is necessary to increase the refrigerant flow rate for the first flow paths 4a and 4b having a large calorific value, and for the second flow path 4c having a small calorific value. Thus, the refrigerant flow rate may be reduced.

According to the first modification, since the refrigerant flow rate F1 from the first inlet 3a1 and the refrigerant flow rate F2 from the second inlet 3a2 can be adjusted, the first flow path that requires more gradual heat is required. Many refrigerants can be supplied to 4a and 4b.
Specifically, in this case, since the refrigerant flow rate U1 in the first cross-sectional area S1 needs to be the same as or higher than the refrigerant flow rate U2 in the second cross-sectional area S2, the condition of U1 ≧ U2 is necessary. , S2 / S1 ≧ F1 / (F1 + F2), the medium flow path 3 may be designed and the flow rates F1 and F2 may be adjusted.

  Further, according to the first modification, since the shape of the medium flow path 3 is changed according to the shape of the reaction flow path 4, the changed part of the shape of the reaction flow path 4, that is, around the merge flow path 4 d It is also possible to adjust the linear velocity of the refrigerant. Moreover, the material which comprises the medium flow path 3 can be reduced, and a reactor body with a low weight can be manufactured.

(Modification 2 of reactor body 1)
Fig.3 (a) is sectional drawing which shows the principal part of reactor main body 1C (1) which concerns on the modification 2 of one Embodiment of this invention.
The reactor main body 1C is different from the above-described reactor main body 1A in terms of the flow direction of the refrigerant. Specifically, the flow direction D1 of the source gas in the reaction flow path 4 is the same as the flow direction D4 of the refrigerant flowing from the inlet 3a toward the outlet 3b (parallel flow).

  As described above, in the direction indicated by the flow direction D1 of the raw material gas, the methanation reaction occurs from a position close to the inlet of the reaction flow path 4, so that the amount of heat generated mainly in the first flow paths 4a and 4b increases. At this time, the refrigerant that has flowed into the medium flow path 3 from the refrigerant supply device 2 through the inlet 3a first cools the first flow paths 4a and 4b, and deprives the first flow paths 4a and 4b of the heat generation amount. In other words, the first flow paths 4a and 4b are cooled at the temperature set by the refrigerant supply device 2. Thereafter, the refrigerant flows toward the second flow path 4c along the same flow direction D4 as the flow direction D1 of the source gas. In the second flow path 4c, since the methanation reaction of most of the source gases has been completed, the amount of heat generated in the second flow path 4c is small. For this reason, even if it is the refrigerant | coolant whose temperature rose comparatively by taking away the emitted-heat amount of 1st flow path 4a, 4b, the 2nd flow path 4c can be cooled.

  According to the second modification, unlike the reactor main body 1A that cools the first flow paths 4a and 4b with the refrigerant that has deprived the calorific value of the second flow path 4c, the refrigerant whose temperature is controlled by the refrigerant supply device 2 is used. Since the first flow paths 4a and 4b are cooled first, the methanation reaction in the first flow paths 4a and 4b having high heat transfer efficiency can be performed efficiently.

(Modification 3 of reactor main body 1)
FIG.3 (b) is sectional drawing which shows the principal part of reactor main body 1D (1) which concerns on the modification 3 of one Embodiment of this invention.
The reactor main body 1D is different from the reactor main body 1B described above in terms of the flow direction of the refrigerant. The medium flow path 3 of the reactor main body 1D has an inlet 3a through which the refrigerant flows into the medium flow path 3, and a first outlet 3b1 and a second outlet 3b2 through which the refrigerant flows out of the medium flow path 3.

  In particular, the flow direction D1 of the source gas in the reaction channel 4 is the same as the flow direction D4 of the refrigerant flowing from the inlet 3a toward the first outlet 3b1 (parallel flow). Further, a part of the refrigerant used for cooling the first flow paths 4a and 4b is discharged from the second outlet 3b2 to the outside of the medium flow path 3 and returns to the refrigerant supply device 2 (flow direction D5), and the rest. The refrigerant is used for cooling the second flow path 4c, is discharged from the first outlet 3b1 to the outside of the medium flow path 3, and returns to the refrigerant supply device 2.

  According to this modification, the first flow paths 4a and 4b are first cooled by the refrigerant whose temperature is controlled by the refrigerant supply device 2 as in the case of the reactor main body 1C, and therefore the first flow path 4a having high heat transfer efficiency. The methanation reaction in 4b can be performed efficiently. Further, since the refrigerant discharged from the second outlet 3b2 returns to the refrigerant supply device 2, the refrigerant supply device 2 preferentially controls the temperature of the refrigerant that has deprived the heat generation amount of the first flow paths 4a and 4b. be able to.

  As mentioned above, although embodiment and modification of this invention were described referring drawings, this invention is not limited to the said embodiment and modification. Various shapes, combinations, and the like of the constituent members shown in the above-described embodiments and modifications are merely examples, and various modifications can be made based on design requirements and the like without departing from the spirit of the present invention.

  For example, in the embodiment and the modification described above, the configuration in which the two first channels 4a and 4b are provided in the reaction channel 4 as the plurality of first channels has been described. Is not limited to two and may be three or more. In this case, the merge channel 4d merges three or more first channels, and supplies the source gas and the methane-containing gas that have circulated through the plurality of first channels to the second channel 4c.

  Moreover, in the said embodiment and modification, although the structure where the one 2nd flow path 4c was provided in the reaction flow path 4 as a 2nd flow path was demonstrated, the number of 2nd flow paths is one. The number is not limited to two and may be two or more. In this case, the number of the first flow paths is smaller than the number of the second flow paths, and a confluence flow path is provided in each of the plurality of second flow paths, and the raw material gas flowing through the plurality of first flow paths Is supplied to each second flow path.

  Moreover, in the said embodiment and modification, a catalyst may be provided not only in the 1st flow paths 4a and 4b and the 2nd flow paths 4c but in the inside of the confluence | merging flow path 4d.

  In the said embodiment and modification, although exothermic reaction (methanation reaction) which produces | generates methane containing gas (target gas) from source gas was demonstrated, this invention is not limited to this. The present invention can be applied to various exothermic reactions or various endothermic reactions other than the methanation reaction. In addition, when applying this invention to endothermic reaction, the heat medium heated rather than the temperature of the reaction field is supplied from a medium supply apparatus to a reactor main body as a temperature control medium.

  In the said embodiment and modification, although the material (type) of the refrigerant | coolant was made the same and the flow volume and temperature were set separately, this invention is not limited to this. All of the refrigerant material (type), flow rate and temperature may be set individually, the material (type) and flow rate may be set individually, and further the material (type) and temperature may be set individually. May be.

  In the above embodiment and the modification, the structure in which the reaction channel 4 is arranged in the medium channel 3 has been described, but the present invention is not limited to this. For example, a coaxial piping structure may be employed. In this case, for example, a structure in which the inner tube, the first intermediate tube, the second intermediate tube, and the outer tube are coaxially arranged from the center toward the outer periphery can be considered. A raw material gas is supplied to the inner pipe and the second intermediate pipe, and a refrigerant is supplied to the first inner pipe and the outer pipe. In this case, the inner pipe corresponds to the first flow path 4a described above, and the second intermediate pipe corresponds to the second flow path 4c described above. The first inner pipe and the outer pipe correspond to the medium flow path 3. The inner pipe and the second middle pipe are joined together by a joining flow path. In such a coaxial piping structure, the second flow path 4c extending from the merge flow path is also provided, and the second flow path 4c is cooled by the refrigerant.

  In the said embodiment and modification, the 1st flow paths 4a and 4b and the 2nd flow path 4c were filled with the catalyst 5, However, This invention is not limited to this. Instead of a filling type catalyst, a coating type catalyst may be used.

  In the said embodiment and modification, although the circulation type refrigerant | coolant supply apparatus was employ | adopted as the refrigerant | coolant supply apparatus 2, this invention is not limited to this. A non-circulating refrigerant supply device that discards the heated refrigerant and sequentially supplies new refrigerant to the reactor main body 1 may be employed as the refrigerant supply device 2.

1, 1A, 1B, 1C, 1D Reactor body 2 Refrigerant supply device 3 Medium flow path 3a Inflow port 3a1 First inflow port 3a2 Second inflow port 3b Outlet 3b1 First outflow port 3b2 Second outflow port 4 Reaction flow channel 4a, 4b First flow path 4c Second flow path 4d Merge flow path 5 Catalyst A Reactors D1, D2, D3, D4, D5 Flow direction

Claims (7)

A reaction apparatus for performing an exothermic reaction or an endothermic reaction,
A plurality of first flow paths; a merge flow path where the plurality of first flow paths merge; and a second flow path connected to the merge flow path; A reaction channel through which a source gas flows in a direction toward the two channels;
A medium flow path through which a temperature adjusting medium for adjusting the temperature inside the reaction flow path flows,
The reaction flow path is provided inside the medium flow path,
The cross-sectional area of each of the plurality of first flow paths is smaller than the cross-sectional area of the second flow path. A catalyst is provided inside each of the plurality of first flow paths and the second flow path,
The reaction apparatus according to claim 1, wherein the catalyst promotes generation of a target gas from the source gas.   The first cross-sectional area of the medium flow path through which the temperature control medium flows at positions corresponding to the plurality of first flow paths is the medium flow through which the temperature control medium flows at positions corresponding to the second flow paths. The reaction apparatus according to claim 1, wherein the reaction apparatus is larger than a second cross-sectional area of the path.   The medium flow path includes a first inlet and a second inlet through which the temperature control medium flows into the medium flow path, and an outlet through which the temperature control medium flows out from the medium flow path. The reaction apparatus according to any one of claims 1 to 3.   The medium channel includes an inlet through which the temperature control medium flows into the medium channel, and a first outlet and a second outlet through which the temperature control medium flows out of the medium channel. The reaction apparatus according to any one of claims 1 to 3. The medium flow path has an inlet through which the temperature control medium flows into the medium flow path, and an outlet through which the temperature control medium flows out from the medium flow path,
The flow direction of the raw material gas in the reaction channel and the flow direction of the temperature control medium flowing from the inlet to the outlet are the same. The reaction apparatus as described in any one of these. The medium flow path has an inlet through which the temperature control medium flows into the medium flow path, and an outlet through which the temperature control medium flows out from the medium flow path,
The flow direction of the source gas in the reaction flow path and the flow direction of the temperature control medium flowing from the inlet to the outlet are opposite to each other. The reaction apparatus as described in any one of these.

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