JP2023040881A - Chemical reaction device and chemical reaction method - Google Patents

Abstract

To provide a chemical reaction device capable of eliminating variations in the temperature of a reaction container with a simple configuration.SOLUTION: In a chemical reaction device 1, raw material is put into a reaction container 2 in a state where a catalyst 3 housed in the reaction container 2 is heated, and a product is discharged from the reaction container 2. The chemical reaction device comprises switching means for switching between a first flow direction in which the raw material is put in from one end side of the reaction container 2 and the product is discharged from the other end side of the reaction container 2 and a second flow direction in which the raw material is put in from the other end side of the reaction container 2 and the product is discharged from the one end side of the reaction container 2.SELECTED DRAWING: Figure 1

Description

The present invention relates to a chemical reaction apparatus and a chemical reaction method for heating a catalyst layer to cause a chemical reaction.

Conventionally, for example, a chemical reaction apparatus is known in which a chemical reaction is performed by circulating a gas in a reaction vessel in a state where a catalyst layer arranged in the reaction vessel is heated by irradiating microwaves ( For example, see Patent Document 1.). In addition, when the object to be heated has temperature characteristics of dielectric properties and the dielectric loss factor increases as the temperature rises, when the temperature distribution occurs even if the object to be heated is a single substance, Microwaves are concentrated in high-temperature areas (hot spots are formed), and as the heating progresses, temperature variation increases, leading to thermal runaway (for example, see Non-Patent Document 1). .

A possible solution to such a problem is, for example, a technique in which a plurality of microwave radiation sources/oscillators are provided and the heating point of the object to be heated is moved by spatial synthesis of electromagnetic waves (for example, non-patent literature 2).

JP 2006-188397 A Noboru Yoshikawa, "Material Microwave Processing and Accompanying Phenomena", [online], Tohoku University Graduate School of Environmental Science, [searched January 10, 2020], Internet <URL: https://www.jstage .jst.go.jp/article/jpi/61/2/61_129/_pdf/-char/ja> "Development of Industrial Microwave Heating Device Using GaN Amplifier Module as Heating Source", [online], New Energy and Industrial Technology Development Organization, Mitsubishi Electric Corporation, Tokyo Institute of Technology, Ryukoku University , Microwave Chemical Co., Ltd., [searched on January 10, 2020], Internet <URL: http://www.mitsubishielectric.co.jp/news/2016/0125.pdf>

However, in the technique described in Non-Patent Document 2, a plurality of oscillators must be provided and the phase of each oscillator must be controlled, which not only increases the manufacturing cost of the device but also complicates the control. There's a problem.

Such a problem of temperature variation can also occur when a chemical reaction is desired to occur within a certain temperature range heated by a heater (electric heater). For example, as shown in FIG. 21, a tubular reaction vessel containing a catalyst is horizontally arranged, and the outer peripheral side of the reaction vessel is heated by a heater. A raw material (to-be-heated material) at room temperature is introduced from the left end port of the reaction vessel, and a reaction product generated by heating and chemical reaction in the reaction vessel is discharged from the right end port of the reaction vessel. In this case, for example, when the length of the reaction vessel is 70 mm, the temperature distribution is as shown in FIG.

Even if the chemical reaction temperature is raised (heater power is increased) to improve the conversion rate, the conversion rate peaks out (saturates) due to the temperature unevenness along the length of the reaction vessel. )Resulting in. On the other hand, if the chemical reaction temperature is too high, overreaction will occur in the high-temperature upper part of the reaction vessel, resulting in increased production of unwanted substances.

SUMMARY OF THE INVENTION Accordingly, an object of the present invention is to provide a chemical reaction apparatus and a chemical reaction method capable of eliminating temperature variations in reaction vessels with a simple configuration.

In order to solve the above-mentioned problems, the invention of claim 1 provides a chemical reaction apparatus in which a raw material is charged into a reaction vessel while a catalyst contained in the reaction vessel is heated, and a product is discharged from the reaction vessel. A first flow direction in which the raw material is introduced from one end side of the reaction vessel and the product is discharged from the other end side of the reaction vessel, and the raw material is introduced from the other end side of the reaction vessel. It is characterized by comprising switching means for switching between a second flow direction in which the product is introduced and discharged from the one end side of the reaction vessel.

The invention according to claim 2 is the chemical reaction apparatus according to claim 1, wherein the heat from the product is transferred to at least one of the one end side and the other end side of the reaction vessel by passing the product. A heat storage unit is provided for storing heat and applying heat to the raw material as the raw material passes through the heat storage unit.

The invention of claim 3 is characterized in that, in the chemical reaction apparatus of claim 2, the heat stored from the product and the heat given to the raw material are cold heat.

The invention according to claim 4 is a chemical reaction method in which raw materials are introduced into the reaction vessel while a catalyst contained in the reaction vessel is heated, and a product is discharged from the reaction vessel, wherein the raw material is subjected to the reaction. A first flow direction in which the product is discharged from the other end of the reaction vessel by charging the product from one end of the reaction vessel, and a flow direction in which the raw material is charged from the other end of the reaction vessel and the product is discharged from the reaction. It is characterized by switching between a second flow direction of discharging from the one end side of the container.

The invention of claim 5 is the chemical reaction method of claim 4, wherein a heat storage unit is provided at least one of the one end side and the other end side of the reaction vessel, and the product passes through the heat storage unit. heat from the product is stored in the heat storage unit, and the heat of the heat storage unit is applied to the raw material by passing the raw material through the heat storage unit.

According to the inventions of claims 1 and 4, the raw material is charged from one end side of the reaction vessel and the product is discharged from the other end side, or the raw material is charged from the other end side of the reaction vessel and the product is discharged. Since it is discharged from one end side, it is possible to eliminate the temperature variation of the reaction vessel. That is, when low-temperature/room-temperature raw materials are introduced from one end of the reaction vessel and high-temperature products are discharged from the other end, one end of the reaction vessel becomes low-temperature and the other end becomes high-temperature. After that, by charging the low-temperature raw material from the other end of the reaction vessel and discharging the high-temperature product from the one end, the temperature of the one end of the reaction vessel rises and the temperature of the other end decreases. In this way, temperature variations in the reaction vessel are eliminated, and as a result, it becomes possible to prevent or suppress the formation of hot spots and thermal runaway, which are problems in the case of heating with microwaves.

In addition, since the temperature variation in the reaction vessel is reduced, the catalyst in the reaction vessel is evenly used, and as a result, it is possible to extend the deterioration life of the catalyst. Moreover, since it is only necessary to switch between the first flow direction and the second flow direction, it is possible to eliminate temperature variations in the reaction vessel with a simple configuration.

According to the inventions of claims 2 and 5, the heat storage unit provided at least one of the one end side and the other end side of the reaction vessel stores heat from the product and gives heat to the raw material. In other words, since the unnecessary heat of the product after the reaction is recovered in the heat storage unit, it is possible to prevent and suppress the generation of unnecessary substances due to overheating, and the recovered heat can be reused to heat the raw materials. Therefore, power consumption required for heating can be reduced.

1 is a conceptual diagram showing an initial state of a chemical reactor according to Embodiment 1 of the present invention; FIG. FIG. 2 is a conceptual diagram showing a first flow state of the chemical reactor of FIG. 1; FIG. 2 is a conceptual diagram showing a second flow state of the chemical reactor of FIG. 1; FIG. 2 is a conceptual diagram showing an experimental device for verifying the principle of the chemical reaction device of FIG. 1; FIG. 5 is a diagram showing experimental results by the experimental apparatus of FIG. 4; 1. It is the apparatus conceptual diagram (a) for verifying the effect of the flow direction switching by the chemical reaction apparatus of FIG. 1, and the figure (b) which shows the simulation result. FIG. 2 is a diagram showing a temperature rise simulation result when the flow direction is switched by the chemical reactor of FIG. 1; FIG. 2 is a diagram showing an example of a processing flow for maximizing a power saving rate in the chemical reaction apparatus of FIG. 1; FIG. 5 is a diagram showing an example of a processing flow in a chemical reactor according to Embodiment 2 of the present invention; FIG. 2 is a conceptual diagram showing an experimental apparatus for verifying a chemical reactor according to Embodiment 2 of the present invention; FIG. 11 is a diagram showing a temperature distribution when only fixed cycle switching is performed in the experimental apparatus of FIG. 10; FIG. 11 is a diagram showing a temperature distribution when only the temperature maximum value switching is performed in the experimental apparatus of FIG. 10; FIG. 11 is a diagram showing a temperature distribution when temperature maximum value switching and fixed cycle switching are used together in the experimental apparatus of FIG. 10 ; FIG. 3 is a conceptual diagram showing a chemical reactor according to Embodiment 3 of the present invention; FIG. 15 is a conceptual diagram showing an experimental device for verifying the principle of the chemical reaction device of FIG. 14; FIG. 16 is a diagram showing a temperature distribution result obtained by the experimental apparatus of FIG. 15; FIG. 17 is a diagram showing the standard deviation of FIG. 16; FIG. 16 is a diagram showing the heat recovery effect of the experimental device of FIG. 15; FIG. 4 is a conceptual diagram showing a chemical reactor according to Embodiment 4 of the present invention; FIG. 2 is a conceptual diagram showing a modification of the chemical reaction device of FIG. 1; It is a conceptual diagram showing a conventional chemical reactor. FIG. 22 is a diagram showing a temperature distribution by the chemical reactor of FIG. 21;

BEST MODE FOR CARRYING OUT THE INVENTION The present invention will be described below based on the illustrated embodiments.

(Embodiment 1)
FIG. 1 is a conceptual diagram showing an initial state of a chemical reactor 1 according to this embodiment. This chemical reaction apparatus 1 is an apparatus in which raw materials are charged into a reaction vessel 2 while a catalyst 3 contained in the reaction vessel 2 is heated, and a reaction product is discharged from the reaction vessel 2. The flow of the raw materials is conventional This point will be mainly described because it is different from the apparatus of Also, in this embodiment, a case where the catalyst 3 is heated by microwave MW will be described.

The reaction vessel 2 is a substantially cylindrical body with both ends closed and contains the catalyst 3, and is arranged so that the axis extends laterally in a microwave heating vessel 4 equipped with a microwave MW radiation source/oscillator. It is Here, the catalyst 3 is a microwave heating catalyst, and is composed of a material with high absorption of microwave MW, for example, a mixture of alumina beads and silicon carbide (SiC), which is a material with high absorption of microwave MW. ing. Both ends of the reaction container 2 protrude from the microwave heating container 4 and are exposed to the outside, and heat storage materials (heat storage units) 31 and 32 are accommodated therein. The heat storage materials 31 and 32 are members that store heat from the product when the product passes through and impart heat to the raw material when the raw material passes therethrough. It is configured. Furthermore, partitions 33 and 34 made of glass wool or the like are arranged between the heat storage materials 31 and 32 and the catalyst 3 .

A first inlet 21 and a first outlet 23 leading to the first heat storage material 31 are provided on one end side of the reaction vessel 2, and a second heat storage material 32 is provided on the other end side. A communicating second inlet 22 and a second outlet 24 are provided. Into such a reaction vessel 2, the raw material is introduced from the first inlet 21 (one end side of the reaction vessel 2) and the product is discharged from the second outlet 24 (the other end side of the reaction vessel 2). and a first flow direction in which the raw material is introduced from the second inlet 22 (the other end side of the reaction vessel 2) and the product is discharged from the first outlet 23 (one end side of the reaction vessel 2). A switching means is provided for switching between the two flow directions.

That is, a first input pipe 41 and a second input pipe 43 are branched from the input port 40, and a first input valve VIN1 is arranged on the input end portion 42 side of the first input pipe 41, and a second input pipe VIN1 is provided. A second injection valve VIN2 is arranged on the injection end portion 44 side of the injection pipe 43 of . A first discharge pipe 51 and a second discharge pipe 53 are branched from the discharge port 50, and a first discharge valve VOUT1 is disposed on the discharge end portion 52 side of the first discharge pipe 51, and a second discharge valve VOUT1 is provided. A second discharge valve VOUT2 is disposed on the discharge end portion 54 side of the discharge pipe 53. As shown in FIG. Also, the input end portion 42 of the first input pipe 41 is connected and communicated with the first input port 21, the input end portion 44 of the second input pipe 43 is connected to the second input port 22, and the first The discharge end 52 of the discharge pipe 51 is connected to the first discharge port 23 , and the discharge end 54 of the second discharge pipe 53 is connected to the second discharge port 24 .

Then, as shown in FIGS. 1 and 2, the first input valve VIN1 and the second discharge valve VOUT2 are opened, the second input valve VIN2 and the first discharge valve VOUT1 are closed, and the raw material is supplied from the input port 40. to form the first flow direction. That is, the raw material passes through the catalyst 3 from one end of the reaction vessel 2 via the first input valve VIN1 and the first heat storage material 31, and is discharged via the second heat storage material 32 and the second discharge valve VOUT2. It is discharged from port 50 . Similarly, as shown in FIG. 3, the second input valve VIN2 and the first discharge valve VOUT1 are opened, the first input valve VIN1 and the second discharge valve VOUT2 are closed, and the material is input from the input port 40. A second flow direction is then formed. That is, the raw material passes through the catalyst 3 from the other end side of the reaction vessel 2 via the second input valve VIN2 and the second heat storage material 32, and passes through the first heat storage material 31 and the first discharge valve VOUT1. It is discharged from the discharge port 50 .

The opening and closing of the input valves VIN1, 2 and the discharge valves VOUT1, 2 are controlled by a control unit (not shown). At this time, the first flow direction and the second flow direction are switched at an appropriate timing, which will be described later, so that the temperature of the reaction vessel 2, that is, the catalyst 3 is substantially uniform over the entire length within a desired temperature range. Control. Further, switching between the first flow direction and the second flow direction is repeated multiple times as necessary.

According to the chemical reaction apparatus 1 having such a configuration, raw materials are charged from one end side of the reaction vessel 2 and products are discharged from the other end side, or raw materials are charged from the other end side of the reaction vessel 2 and produced Since the material is discharged from one end side, it is possible to eliminate the temperature variation of the reaction vessel 2, that is, the catalyst 3. That is, as shown in FIGS. 1 and 2, when low-temperature/room-temperature raw materials are introduced from one end of the reaction vessel 2 and high-temperature products are discharged from the other end, one end of the reaction vessel 2 becomes low-temperature and the other end side becomes hot. After that, as shown in FIG. 3, by charging the low temperature raw material from the other end side of the reaction vessel 2 and discharging the high temperature product from the one end side, the temperature of the one end side of the reaction vessel 2 is increased and the temperature of the other end side is decreased. do. In this way, the temperature variation of the reaction vessel 2 is eliminated, and as a result, it is possible to prevent and suppress the formation of hot spots and thermal runaway, which are problems in the case of heating with microwave MW.

In addition, since the temperature variation in the reaction vessel 2 is reduced, the catalyst 3 in the reaction vessel 2 is evenly used, and as a result, the degradation life of the catalyst 3 can be extended. Moreover, since it is only necessary to switch between the first flow direction and the second flow direction, it is possible to eliminate temperature variations in the reaction vessel 2 with a simple configuration.

Furthermore, heat storage materials 31 and 32 provided at both ends of the reaction vessel 2 store heat from the product and provide heat to the raw material. That is, since unnecessary heat of the product after the reaction is recovered by the heat storage materials 31 and 32, it is possible to prevent and suppress the generation of unnecessary substances due to overheating, and the recovered heat is used to heat the raw material. It is possible to reduce power consumption required for heating.

Next, principle verification of the chemical reaction device 1 will be described. First, in the experimental apparatus shown in FIG. 4 (with only one heat storage material), which has the same configuration as the chemical reaction apparatus 1, the microwave power is kept constant and the air is flowed in a single direction (FORWARD direction). 5, "unidirectional flow", the temperature of the microwave heating element, ie, the catalyst 3, increases by 325K. On the other hand, when the air flow direction was switched to the REVERSE direction at intervals of 60 seconds, the temperature of the catalyst 3 further increased by 50 K, as indicated by "channel switching" in FIG. In other words, the effect of switching the flow direction and heat recovery by the heat storage material was confirmed.

In addition, in the simulation model of the experimental apparatus of FIG. 6A, which has the same configuration as the chemical reaction apparatus 1, the reaction part (catalyst FIG. 6B shows the transient calculation result of the temperature distribution in 3). As shown in this figure, it was confirmed that the maximum temperature position of the reaction vessel 2 moved from the steady temperature distribution L1 in the unidirectional flow to the temperature distribution L4 after 75 seconds. In other words, it was confirmed that the formation of localized hot spots was prevented and suppressed. Also, from FIG. 6(b), it is clear that temperature variations in the temperature distributions L2, L3, and L4 after reversing the flow direction are reduced as compared with the temperature distribution L1 of the unidirectional flow.

Further, FIG. 7 shows the calculation result of the average temperature of the catalyst 3 when the flow direction is switched multiple times from the "unidirectional flow" state when the length of the heat storage materials 31 and 32 is 1 m. A temperature rise of about 250 K was observed by switching three times, and the power saving rate ((1-(temperature rise from room temperature in unidirectional flow) / (temperature rise from room temperature in flow channel switching)) x 100%). was calculated to have an average of about 30% and a maximum of 37.5%. Further, from this figure, it can be considered that the power saving rate can be maximized by switching the flow direction at the timing CP when the differential value of the temperature rise curve becomes zero (no temperature rise). FIG. 8 shows the processing flow of this temperature maximum value switching. However, the timing is not limited to this method, the first flow direction is switched to the maximum temperature value, the second flow direction is switched at the same timing as the first flow direction, or vice versa, fixed time switching, reaction vessel 2 pressure fluctuations, changes in heater heating power, changes in resonance frequency in the case of microwave heating, and optimum times calculated by machine learning can be used.

(Embodiment 2)
This embodiment exemplifies a case in which both the maximum temperature value switching and the fixed cycle switching with a fixed switching cycle are used. Here, in this embodiment, the case where the heating means is a heater will be described as an example, as in the case of the third embodiment which will be described later.

That is, as shown in FIG. 9, the first round trip after starting flow switching is the second flow direction (REVERSE direction) state as the first extremum search process P1 as in FIG. 8 above. , the elapsed time ta until the heater temperature Ti reaches the temperature maximum value (extreme value) is searched. Subsequently, similarly, as the second extremum search process P2, the elapsed time tb until the heater temperature Tj reaches the temperature maximum value in the first flow direction (FORWARD direction) is searched.

Next, from the second round trip after the start of flow path switching, scaling (for example, 0.7 to 0.9 ), and the switching time is gradually shortened for each reciprocation of the flow path switching. Repeat until the desired time (eg, set to 5-30 seconds) is reached. Here, the condition for exiting this loop may be that the temperature difference between the heat storage material temperature symmetry points, which will be described later, approaches within a predetermined range.

Subsequently, in the final process P4 after the set minimum value reaching process P3, in the second flow direction (REVERSE direction), the elapsed time tc until the heater temperature Tk reaches the temperature maximum value is searched, and the flow path is reversed. In the first flow direction (FORWARD direction) state, the switching loop of maintaining the flow for the previously searched time tc is repeated until the operation is stopped.

In this way, by using both the maximum temperature value switching and the fixed period switching, the time to reach a steady state after switching the flow path is short, and the temperatures of both heat storage materials become bilaterally symmetrical (equal temperature distribution ), it is possible to obtain the advantage that the power saving rate is high. For example, in the experimental apparatus shown in FIG. 10, when only fixed cycle switching (period of 15 seconds) is performed, the temperatures of both heat storage materials become bilaterally symmetrical when a steady state is reached by channel switching, as shown in FIG. On the other hand, when only the maximum temperature value is switched in the experimental apparatus shown in FIG. 10, the maintenance time in the first flow direction and the maintenance time in the second flow direction are different, Material temperature is not symmetrical.

On the other hand, in the experimental apparatus shown in FIG. 10, when the temperature maximum value switching and the fixed period switching are used together, when the steady state is reached by the flow path switching, the temperature of both heat storage materials changes left and right as shown in FIG. It can be confirmed that the time required to reach a steady state is short while being targeted. Here, the extreme value search processes P1 and P2 correspond to P1 and P2 in FIG. 13, the set minimum value reaching process P3 corresponds to P3 in FIG. 13, and the final process P4 corresponds to P4 in FIG. Applicable.

(Embodiment 3)
FIG. 14 is a conceptual diagram showing a chemical reactor 10 according to this embodiment. In this embodiment, the heater (electric heater) 6 is used to heat the reaction vessel 2, that is, the catalyst 3, and the heating means differs from that in the first embodiment. The description is omitted by adding

That is, in this embodiment, the heater 6 is arranged so as to cover the portion (central portion) of the reaction vessel 2 containing the catalyst 3 . Also with such a configuration, the same effects as those of the first embodiment can be obtained. In other words, it is possible to reduce temperature variations over the entire length of the reaction vessel 2, extend the deterioration life of the catalyst 3, and prevent or suppress the generation of unnecessary substances due to overheating. At the same time, it is possible to reduce power consumption required for heating.

Next, the temperature change of each part of the heater 6 when the heater power is constant and the flow direction is switched in the experimental apparatus of FIG. 16 and its standard deviation SD is shown in FIG. Here, in FIG. 16, the curve L11 indicates the temperature change on the inlet side of the heater 6 (the left side in FIG. 15, the input side in the first flow direction), and the curve L12 indicates the temperature change on the central portion of the heater 6. , and a curve L13 shows the temperature change on the outlet side of the heater 6 (the right side in FIG. 15, the inlet side in the second flow direction). From these figures, it was confirmed that by switching the flow direction, the temperature of the heater 6 rises over the entire length, and the standard deviation, that is, the temperature variation, is compressed to about 1/3 at maximum.

18, the average temperature of the heater 6 rises by 100 K when the air flows in one direction (FORWARD direction). The temperature rose another 57K. In other words, the effect of switching the flow direction and heat recovery by the heat storage material was confirmed. In this case, a power saving rate of about 36.3 (=1-100/157)% can be expected.

(Embodiment 4)
FIG. 19 is a conceptual diagram showing a chemical reactor 11 according to this embodiment. This embodiment differs from the first embodiment in that a liquid substance 70 is contained as a reactant in the reaction vessel 2 instead of the catalyst 3. The description is omitted by attaching the same reference numerals.

In this embodiment, heat storage materials (heat storage units) 71 and 72 having a honeycomb structure are accommodated at both ends of the reaction vessel 2 as necessary so as not to block the flow (pipe blockage). Here, as an example of the mixture of liquid and solid continuously fed from the feeding port 40, pretreatment for bioethanol production from woody biomass is performed to decompose lignin, and liquid substances (woody biomass, water, organic A mixture of solvents) is heated at 200° C. to decompose lignin.

Although the embodiments of the present invention have been described above, the specific configuration is not limited to the above-described embodiments. Included in the invention. For example, in the above embodiment, the reaction vessel 2 is arranged so as to extend horizontally, but it may be arranged so as to extend vertically. In addition, although the heat storage materials 31 and 32 are accommodated on both end sides of the reaction vessel 2, depending on the desired temperature range in which the reaction vessel 2 is to be uniformly heated, one end side or the other end side of the reaction vessel 2 may be used. can be accommodated only in

Further, for example, in Embodiment 1, a three-way valve 35 as shown in FIG. 20 may be connected to the end of the reaction vessel 2 whose both ends are open to control the flow of raw materials and products. . Also, the heat stored by the heat storage materials 31, 32, 71, 72 from the product and the heat given to the raw material may be cold heat.

Reference Signs List 1, 10, 11 chemical reactor 2 reaction vessel 21, 22 inlet 23, 24 outlet 3 catalyst 31, 32 heat storage material (heat storage unit)
4 Microwave heating container 40 Input port 41, 43 Input pipe 42, 44 Input end 50 Ejection port 51, 53 Ejection pipe 52, 54 Ejection end 6 Heater (heating means)
70 liquid 71, 72 heat storage material (heat storage unit)
VIN1, 2 Input valve (switching means)
VOUT1, 2 discharge valve (switching means)
MW microwave (heating means)

Claims (5)

A chemical reaction apparatus in which a raw material is put into the reaction vessel while the catalyst contained in the reaction vessel is heated, and a product is discharged from the reaction vessel,
A first flow direction in which the raw material is charged from one end of the reaction vessel and the product is discharged from the other end of the reaction vessel, and a first flow direction in which the raw material is charged from the other end of the reaction vessel and Switching means for switching between a second flow direction in which the product is discharged from the one end side of the reaction vessel,
A chemical reactor characterized by: At least one of the one end side and the other end side of the reaction vessel is provided with a heat storage unit that stores heat from the product when the product passes therethrough and imparts heat to the raw material when the raw material passes therethrough. is provided,
The chemical reaction apparatus according to claim 1, characterized by: The heat stored from the product and the heat imparted to the feedstock is cold.
3. The chemical reactor according to claim 2, characterized by: A chemical reaction method in which raw materials are introduced into the reaction vessel while the catalyst contained in the reaction vessel is heated, and the product is discharged from the reaction vessel,
A first flow direction in which the raw material is charged from one end of the reaction vessel and the product is discharged from the other end of the reaction vessel, and a first flow direction in which the raw material is charged from the other end of the reaction vessel and switching between a second flow direction that discharges product from the one end of the reaction vessel;
A chemical reaction method characterized by: A heat storage unit is provided on at least one of the one end side and the other end side of the reaction vessel, and heat from the product is stored in the heat storage unit as the product passes through the heat storage unit, and the raw material is supplied to the heat storage unit. applying the heat of the heat storage unit to the raw material by passing through the heat storage unit;
5. The chemical reaction method according to claim 4, characterized in that:

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