JP2021155242A - Reformer and reformation treatment apparatus - Google Patents

Abstract

To provide a reformer capable of changing and adjusting a temperature of a reformed gas discharged from a reaction tube and a temperature of a reformed gas discharged from a lower side of a filling part of the reaction tube.SOLUTION: The reformer is characterized in that a reaction tube A is provided in which an inner tube 4 in which a bottom is opened is formed inside an outer tube 3 in which a bottom is closed, and a filling portion filled with a catalyst S is formed between the outer tube 3 and the inner tube 4, and the inner tube 4 is constituted of an outer inner tube 4a facing the outer tube 3 and an internal inner tube 4b arranged inside of the outer inner tube 4a, and between the outer inner tube 4a and the internal inner tube 4b, a heating flow path Qa for flowing a reformed gas K discharged from the lower side of the filling part toward the above is provided, inside of the internal inner tube 4b, a bypass flow path Qb for flowing the reformed gas K discharged from the lower side of the filling part toward the above is provided, and a control part for controlling heating flow amount for flowing the reformed gas K through the heating flow pass Qa and the bypass flow pass flow amount for flowing the reformed gas K through the bypass flow pass Qb is provided.SELECTED DRAWING: Figure 3

Description

In the present invention, an inner pipe having an open bottom is arranged inside an outer pipe whose bottom is closed, and a filling portion filled with a catalyst between the outer pipe and the inner pipe is formed in a vertically oriented posture. A modified reaction tube is provided, a raw material gas supply section for supplying a hydrocarbon-based raw material gas mixed with water vapor is provided on the upper side of the filling section, and a combustion section for heating the outer surface of the outer tube. The present invention relates to a pawnbroker and a reformer processing apparatus provided with the reformer.

Such a reformer reforms steam by supplying a raw material gas, which is a hydrocarbon-based gas such as natural gas or naphtha, in a state of being mixed with steam between the outer tube and the inner tube in the reaction tube. It will be used to reform the raw material gas into a reformed gas with a large amount of various components, such as reforming to a reformed gas with a large amount of hydrogen components by treatment.

As a conventional example of such a reformer, there is one configured to flow and discharge the entire amount of the reformed gas containing a large amount of hydrogen component discharged from the lower side of the filling portion upward through the inside of the inner pipe. (See, for example, Patent Document 1.).

Incidentally, although not described in Patent Document 1, in addition to the reformer, a desulfurizer that desulfurizes the raw material gas supplied to the reformer and a reformer gas discharged from the reformer are modified. A reforming processing apparatus for generating a modified gas having a large amount of hydrogen gas and a low CO concentration is provided by providing a CO transforming device for processing.

Special Fair 6-69882 Gazette

In a reforming apparatus equipped with a reformer, the temperature of the heating operation gas discharged from the reformer is made as high as possible in the heating operation state in which the operation is started from the stopped state, and the CO transformer is used. It is desired to promote the temperature rise of the CO transformer by flowing the high-temperature temperature-raising operation gas.
In general, a desulfurizer is provided so that heat can be exchanged with the CO transformer, and the temperature of the desulfurizer is raised at the same time as the temperature of the CO transformer is raised.

By the way, as the gas for the temperature raising operation, when the raw material gas is supplied to the desulfurizer from the start of the operation, the reformed gas becomes the gas for the temperature raising operation and flows over the desulfurizer, the reformer and the CO metamorphic device. When the road is filled with hydrogen gas, a gas different from the reformed gas may be used as the temperature raising operation gas, for example, the hydrogen gas becomes a temperature rising operation gas. , The explanation will be continued assuming that the gas for heating temperature operation is a reformed gas.

In the conventional reformer, the entire amount of the heating operation gas discharged from the lower side of the filling portion is configured to flow upward through the inside of the inner pipe and discharged, so that the reaction is carried out. To raise the temperature of the heating operation gas discharged from the pipe, that is, the temperature of the heating operation gas discharged from the reformer, increase the combustion amount of the combustion part and lower the filling part. The temperature of the temperature raising operation gas discharged from the side will be raised.

However, for the purpose of suppressing overheating of the filled part filled with the catalyst, the target temperature is the temperature on the bottom side inside the reaction tube, which corresponds to the temperature of the heating operation gas discharged from the lower side of the filled part. As a result, the temperature of the temperature raising operation gas discharged from the lower side of the filling portion cannot be raised to a high temperature.

Further, when the reformer is configured in such a form that a plurality of reaction tubes are arranged side by side, such as by arranging a plurality of reaction tubes in parallel around the combustion part, the raw material gas is branched and supplied to the plurality of reaction tubes. Due to the bias in the branch supply amount and the like, the temperature of the reformed gas discharged from the lower side of the filling portion in the plurality of reaction tubes may differ.

In such a case, it is necessary to keep the bottom side temperature inside the reaction tube corresponding to the temperature of the reforming gas discharged from the lower side of the filling part to be equal to or lower than the target temperature. Since the combustion amount of the combustion part is controlled so as to maintain the highest temperature at the target temperature, the temperature of the reforming gas discharged from the lower side of the filling part becomes lower than the target temperature. Due to the formation of pipes and the like, it is difficult to properly perform the steam reforming treatment in all the reforming pipes, and there is a disadvantage that it is difficult to increase the treatment amount of the reforming gas.

The present invention has been made in view of the above circumstances, and an object of the present invention is the temperature of the reforming gas discharged from the reaction tube and the temperature of the reforming gas discharged from the lower side of the filling portion of the reaction tube. The point is to provide a reformer capable of changing and adjusting the temperature, and a reforming processing apparatus equipped with the reformer.

In the reformer of the present invention, an inner pipe having an opening at the bottom is arranged inside the outer pipe having a closed bottom, and a filling portion filled with a catalyst between the outer pipe and the inner pipe is arranged in the vertical direction. The reaction tube formed in the facing posture and
A raw material gas supply unit that supplies a hydrocarbon-based raw material gas mixed with water vapor to the upper side of the filling unit, and a raw material gas supply unit.
A combustion part that heats the outer surface of the outer pipe is provided, and the characteristic configuration thereof is as follows.
The inner pipe is composed of an outer inner pipe facing the outer pipe and an inner inner pipe arranged inside the outer inner pipe.
A heating flow path is provided between the outer pipe and the outer inner pipe to allow the reformed gas discharged from the lower side of the filling portion to flow upward and discharge from the reaction pipe.
Inside the inner inner pipe, a bypass flow path is provided in which the reformed gas discharged from the lower side of the filling portion is allowed to flow upward and discharged from the reaction pipe.
A point that is provided with an adjusting unit that adjusts the amount of heating flow that causes the reformed gas discharged from the lower side of the filling unit to flow through the heating flow path and the amount of bypass flow that flows through the bypass flow path. It is in.

That is, when the reforming gas discharged from the lower side of the filling portion is flowed upward through the heating flow path formed between the outer inner pipe and the inner inner pipe and discharged from the reaction pipe. Since the amount of heat of the reforming gas discharged from the lower side of the filling part can be efficiently given to the filling part of the catalyst through the outer inner pipe, the temperature of the reforming gas discharged from the lower side of the filling part rises. However, the temperature of the reforming gas discharged from the reaction tube tends to decrease.

On the other hand, when the reforming gas discharged from the lower side of the filling part is allowed to flow upward through the bypass flow path formed inside the inner inner pipe and discharged from the reaction pipe, the filling part is discharged. Since the calorific value of the reforming gas discharged from the lower side of the filling portion is transmitted to the outer and inner pipes via the heating flow path, the calorific value of the reforming gas discharged from the lower side of the filling portion is filled with the catalyst. Since it cannot be efficiently given to the portion, the temperature of the reforming gas discharged from the lower side of the filling portion tends to decrease, and the temperature of the reforming gas discharged from the reaction tube tends to increase.

Therefore, the adjusting unit adjusts the heating flow amount for flowing the reformed gas discharged from the lower side of the filling part through the heating flow path and the bypass flow amount for flowing through the bypass flow path from the reaction tube. The temperature of the reformed gas discharged and the temperature of the reformed gas discharged from the lower side of the filling part of the reaction tube can be changed and adjusted.

In short, according to the characteristic configuration of the reformer of the present invention, the temperature of the reformed gas discharged from the reaction tube and the temperature of the reformed gas discharged from the lower side of the filling portion of the reaction tube can be changed and adjusted.

A further characteristic configuration of the reformer of the present invention is that a temperature detection unit for detecting the temperature of the bottom side portion of the reaction tube is provided.
The point is that the operation control unit executes a temperature control process for controlling the combustion amount of the combustion unit in order to maintain the temperature of the temperature detection unit at the target temperature.

That is, the operation control unit executes the temperature control process for controlling the combustion amount of the combustion unit in order to maintain the temperature of the temperature detection unit that detects the temperature of the bottom side portion of the reaction tube at the target temperature. The packed portion filled with the catalyst can be appropriately heated while suppressing overheating of the filled portion filled with the catalyst.

Therefore, by appropriately heating the packed portion filled with the catalyst, the steam reforming treatment can be appropriately performed and the reformed gas can be satisfactorily generated.

In short, according to the further characteristic configuration of the reformer of the present invention, the filled portion filled with the catalyst can be appropriately heated while suppressing overheating of the filled portion filled with the catalyst.

A further characteristic configuration of the reformer of the present invention is that a plurality of the reaction tubes are juxtaposed in a state where the raw material gas is branched and supplied.
The temperature at which the operation control unit increases the bypass flow amount for the reaction tube having a high temperature in order to reduce the higher temperature among the temperatures detected by the temperature detection unit in each of the plurality of reaction tubes. A point of executing a lowering process and, as the temperature control process, a process of maintaining the highest temperature among the temperatures detected by the temperature detection unit in each of the plurality of reaction tubes at the target temperature. It is in.

That is, in order to reduce the higher temperature among the temperatures detected by the temperature detection units in each of the plurality of reaction tubes, the operation control unit performs a temperature reduction process for increasing the bypass flow amount for the reaction tubes having the higher temperature. Since it is executed, it is detected by the temperature detectors in each of the plurality of reaction tubes, such that the extremely high temperature does not exist among the temperatures detected by the temperature detectors in each of the plurality of reaction tubes. It is possible to average the temperature.

Then, as a temperature control process in which the operation control unit controls the combustion amount of the combustion unit in order to maintain the temperature of the temperature detection unit at the target temperature, the temperature detected by the temperature detection unit in each of the plurality of reaction tubes Since the process of maintaining the highest temperature among them is executed at the target temperature, it is possible to heat the filled portion to an appropriate temperature while suppressing overheating of the filled portion of the catalyst in each of the plurality of reaction tubes. It is possible to increase the amount of reformed gas produced while appropriately performing the steam reforming treatment in each of the plurality of reaction tubes.

In short, according to the further characteristic configuration of the reformer of the present invention, it is possible to increase the amount of reformed gas produced while appropriately performing the steam reforming treatment in each of the plurality of reaction tubes. ..

The reforming apparatus of the present invention includes the above-mentioned reformer, and its characteristic configuration is as follows.
The raw material gas is a gas desulfurized by a desulfurizer and mixed with steam, and the reformed gas discharged from the reformer is supplied to the CO metamorphic part.
The point is that the operation control unit executes a bypass flow process that controls the adjustment unit so that the bypass flow amount becomes larger than the heating flow amount in the temperature rise operation state in which the operation is started from the operation stop state. ..
Incidentally, the "state in which the bypass flow amount is larger than the heating flow amount" in the above description is a state in which each of the bypass flow amount and the heating flow amount exists, or the heating flow amount is set to zero and the bypass flow amount is set to zero. It includes the state in which only exists.

That is, since the raw material gas supplied to the reformer is a gas that has been desulfurized in the reformer and mixed with steam, the steam reforming treatment in the reformer is performed satisfactorily while suppressing deterioration of the catalyst. In addition, since the reformed gas discharged from the reformer is supplied to the CO reforming part, carbon monoxide contained in the reformed gas is transformed into carbon dioxide. , A modified gas having a large amount of hydrogen gas components and a low CO concentration can be appropriately generated.

Then, the operation control unit executes the bypass flow process in the temperature rise operation state in which the operation is started from the stopped state, so that the bypass flow amount of the reformed gas flowing in the bypass path inside the inner inner pipe is increased. Since the amount of heating flow of the reforming gas flowing in the heating flow path between the outer and inner pipes becomes larger than the heating flow amount of the reforming gas, the temperature of the reforming gas discharged from the reaction tube, that is, reforming It is possible to raise the temperature of the reforming gas discharged from the vessel.

By the way, if the bypass flow amount is larger than the heating flow amount, the temperature of the reforming gas discharged from the lower side of the filling part will decrease, and the temperature detection unit that detects the temperature of the bottom side part of the reaction tube. However, if the operation control unit executes the temperature control process, the combustion amount of the combustion unit will increase in order to maintain the temperature of the temperature detection unit at the target temperature, and it will be discharged from the reformer. It is possible to further increase the temperature of the reforming gas to be produced.

Then, when the temperature of the reforming gas discharged from the reformer becomes high, the temperature rise of the CO transformer can be promoted by flowing the high-temperature reforming gas through the CO transformer. If the desulfurizer is provided so that heat can be exchanged with the CO transformer, the temperature of the desulfurizer can be raised at the same time as the temperature of the CO transformer is raised, and as a result, the operation is started from the stopped state. When the temperature raising operation is performed, the operation time can be shortened.

In short, according to the characteristic configuration of the reforming processing apparatus of the present invention, it is possible to shorten the operation time when performing the temperature raising operation in which the operation is started from the stopped state.

It is a vertical sectional front view which shows the reforming furnace. It is a top view which shows the arrangement form of the reaction tube in a reforming furnace. It is a partially omitted longitudinal front view showing a reaction tube. It is a schematic block diagram of a hydrogen production apparatus. It is a figure which shows the flow state of the gas during the standby operation of a hydrogen production apparatus. It is a graph which shows the change state of temperature.

[Embodiment]
Hereinafter, embodiments of the present invention will be described with reference to the drawings.
(Overall configuration of reformer)
As shown in FIG. 1, the reformer H reforms a hydrocarbon-based raw material gas G such as natural gas or naphtha into a reformed gas K having a large hydrogen component by steam reforming, and reacts. A reforming furnace 2 equipped with a tube A and a burner B for heating the reaction tube A is provided.
Incidentally, as will be described later, the reformer H is provided in the reforming unit R (an example of the reforming treatment device, see FIG. 4) including the desulfurizer 12, and the raw material gas G is the desulfurizer 12. After desulfurization treatment, steam is mixed with the raw material gas G after the desulfurization treatment, and the raw material gas G mixed with the steam is supplied to the reformer H.

The reformer 2 is configured to include an upper wall 2U, a bottom wall 2D, and a cylindrical side wall 2S arranged between the upper wall 2U and the bottom wall 2D.
Then, the burner B is provided in the central portion of the upper wall 2U of the reformer H so as to burn downward, and the discharge portion 2E for discharging the combustion gas E of the burner B is opened at the upper portion of the side wall 2S. ing.

As shown in FIGS. 1 and 2, a plurality of reaction tubes A are provided in a posture of hanging from the upper wall 2U of the reformer H and arranged side by side at intervals along the periphery of the burner B. Has been done.
In the present embodiment, the case where four reaction tubes A are provided as a plurality of reaction tubes A is illustrated, but it may be carried out in a form in which three or five or more reaction tubes A are provided.

Further, as shown in FIG. 1, a cylindrical outer wall 2G is provided at a location on the outer side of the side wall 2S of the reformer H in a state of being arranged between the upper wall 2U and the bottom wall 2D. ing.
Then, in the external space F between the side wall 2S and the outer wall 2G, a steam generating heat exchanger J that generates steam to be mixed with the raw material gas G supplied to the upper part of the reaction tube A is arranged, and the outside An external discharge port 2Z for discharging the combustion gas E flowing from the discharge portion 2E through the external space F is provided at a location on the lower side of the square wall 2G.

Further, as shown in FIG. 1, an air preheating heat exchanger N for preheating the air supplied to the burner B is provided between the steam generation heat exchanger J and the outer wall 2G in the external space F. There is.

(Details of reaction tube)
As shown in FIG. 3, the reaction tube A includes an outer tube 3 whose bottom is closed and an inner tube 4 arranged inside the outer tube 3, and the inner tube 4 is in a state of opening the bottom. A filled portion filled with the granular catalyst S is formed between the outer tube 3 and the inner tube 4 in a vertical direction.
The upper end side portion of the outer pipe 3 is supported by the upper wall 2U in a state of penetrating the upper wall 2U of the reformer H, and the upper end side portion of the inner pipe 4 penetrates the pipe upper wall 3u of the outer pipe 3. In the state, it is supported by the pipe upper wall 3u.

A porous catalyst support portion T that receives and supports the catalyst S is provided between the outer tube 3 and the inner tube 4.
The catalyst support portion T is provided with a flow hole U for passing a reforming gas K (an example of a processing gas) that flows between the outer pipe 3 and the inner pipe 4 toward the bottom side of the outer pipe 3. It is formed and supported by the lower end of the inner tube 4.
Incidentally, in FIG. 3, as the catalyst support portion T, a perforated plate-like form in which the flow holes U are formed over the entire surface is illustrated. For example, the flow holes U are arranged in a row along the circumferential direction. As long as the catalyst support portion T is provided with a flow hole U for receiving the catalyst S and allowing the reformed gas K to pass therethrough, the catalyst support portion T is formed in a plate-like shape formed in a state of being lined up with each other. Can be configured in form.

In the present embodiment, the inner pipe 4 is configured as a double pipe including an outer inner pipe 4a facing the outer pipe 3 and an inner inner pipe 4b arranged inside the outer inner pipe 4a. The catalyst S is filled between 4a and the outer tube 3.
Further, the catalyst support portion T is supported by the bottom portion of the outer inner tube 4a.
That is, a heating flow path in which the reformed gas K discharged from the lower side of the filling portion of the catalyst S flows upward between the outer and inner pipes 4a and the inner inner pipe 4b and is discharged from the reaction pipe A. Qa is provided.
Further, inside the inner inner pipe 4b, a bypass flow path Qb is provided in which the reformed gas K discharged from the lower side of the filling portion of the catalyst S is allowed to flow upward and discharged from the reaction pipe A.

A raw material gas pipe 5 for introducing a raw material gas G mixed with steam is connected to a portion of the outer pipe 3 protruding from the upper wall 2U of the reformer H. That is, the raw material gas pipe 5 corresponds to the raw material gas supply unit that supplies the raw material gas G mixed with water vapor to the upper side of the filling portion of the catalyst S.
Although not shown, the raw material gas pipe 5 is provided in a state of being branched into a plurality (4) toward the outer pipes 3 of each of the plurality (4) reaction tubes A.
Incidentally, as will be described later, the steam generated by the heat exchanger J for steam generation is supplied to the raw material gas pipe 5, and the raw material gas G and the steam are mixed through the raw material gas pipe 5. It will be supplied to the outer pipe 3 in this state.

A main guide pipe 6A for guiding the reformed gas K is connected to a portion of the inner pipe 4 that protrudes from the pipe upper wall 3u of the outer pipe 3. That is, the reformed gas K flowing through the heating flow path Qa is discharged from the reaction tube A through the main guide tube 6A.
Further, the extension cylinder portion 9 is provided on the upper wall portion 4u of the inner pipe 4 so as to project upward, so that the internal space of the extension cylinder portion 9 and the internal space of the inner inner pipe 4b communicate with each other. Has been done.
An auxiliary guide pipe 6B for guiding the reformed gas K is connected to the extension cylinder portion 9. That is, the reformed gas K flowing through the bypass flow path Qb is discharged from the reaction tube A through the auxiliary guide tube 6B.

Further, as shown in FIG. 1, the auxiliary guide pipe 6B is connected to the main guide pipe 6A in a confluent state.
Then, the plurality of main guide pipes 6A extending from each of the plurality of reaction pipes A are merged and connected to a single reforming gas pipe 6 on the downstream side of the connection point of the auxiliary guide pipe 6B. ..

As shown in FIG. 1, the main guide pipe 6A is provided with a main adjusting valve 6s that adjusts the opening degree of the main guide pipe 6A from a fully closed state to a fully open state, and the auxiliary guide pipe 6B is provided with the main adjusting valve 6s. An auxiliary adjusting valve 6h for adjusting the opening degree of the auxiliary guide pipe 6B from the fully closed state to the fully open state is provided.
An adjustment unit that adjusts the amount of heating flow from the main control valve 6s and the auxiliary control valve 6h to allow the reforming gas K to flow through the heating flow path Qa and the amount of bypass flow to flow the reforming gas K through the bypass flow path Qb. 6V is configured.

That is, the raw material gas G mixed with steam is supplied from the raw material gas pipe 5 between the outer pipe 3 and the outer inner pipe 4a, and the filling portion of the catalyst S between the outer pipe 3 and the outer inner pipe 4a. By flowing downward through, the reformed gas K is reformed into a reformed gas K having a large hydrogen component by the steam reforming treatment, and the reformed gas K is discharged from the filling portion of the catalyst S through the catalyst support portion T. It will flow to the bottom side of the outer pipe 3.

After that, the reforming gas K flowing to the bottom side of the outer pipe 3 flows to the upper side through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b, and is discharged through the main guide pipe 6A. Alternatively, the reformed gas K that flows upward through the bypass flow path Qb in the internal space of the inner inner pipe 4b and is discharged through the auxiliary guide pipe 6B is the main guide. It will flow into the reformed gas pipe 6 in a state where it joins the pipe 6A.

Incidentally, the reforming gas K is filled between the outer pipe 3 and the outer inner pipe 4a by a configuration in which the reforming gas K flows upward through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. A heat exchange unit for heating the catalyst S is configured.
That is, since the reforming gas K flowing to the bottom side of the outer pipe 3 is in a high temperature state (for example, 800 ° C.), the reforming gas K in this high temperature state is used between the outer pipe 3 and the outer inner pipe 4a. It is configured to heat the catalyst S filled in.

Then, the reforming gas K that has flowed to the bottom side of the outer pipe 3 is flowed to the upper side through the bypass flow path Qb formed in the internal space of the inner inner pipe 4b, so that the heat exchange function by the heat exchange unit is performed. Is configured to reduce.
Specifically, the bypass flow amount of the reforming gas K that flows to the upper side through the bypass flow path Qb is changed to flow to the upper side through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. The heat exchange function of the heat exchange section is lowered as the amount of the quality gas K is larger than the heating flow amount, and as a result, the temperature of the reformed gas K after merging is set to be high.

In the following description, the reformed gas K that flows upward through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b and is discharged through the main guide pipe 6A is, if necessary. The reforming gas K for heat exchange, which is called the reforming gas K for heat exchange, flows upward through the bypass flow path Qb in the internal space of the inner inner pipe 4b and is discharged through the auxiliary guide pipe 6B. The reformed gas K which is referred to as gas K and flows downstream of the connection point of the auxiliary guide pipe 6B in the main guide pipe 6A is referred to as reformed gas K after merging, if necessary.

The heating flow amount of the reformed gas K for heat exchange and the pipe pass flow amount of the reformed gas K for bypass are changed and adjusted by adjusting the opening degree between the main control valve 6s and the auxiliary control valve 6h.
Incidentally, as shown in FIG. 1, an operation control unit M for controlling the operation of the hydrogen production apparatus described later is provided, and the operation control unit M opens the main control valve 6s and the auxiliary control valve 6h as described later. It is configured to make degree adjustments.

(About temperature control)
As shown in FIG. 3, a state in which the temperature measuring cylinder 8 (an example of the temperature detection unit) penetrates the inside of the inner pipe 4 up and down (in the present embodiment, penetrates the inside of the inner pipe 4b up and down). It is installed in the state).
That is, a connecting flange 9A is provided at the upper end of the extension cylinder portion 9 described above.
The cylinder side flange 8A that holds the temperature measurement cylinder 8 by a swedge lock joint or the like is detachably bolted to the connecting flange 9A.

The temperature measuring cylinder 8 is inserted so that its lower end is adjacent to the bottom of the outer tube 3, and a temperature measuring element (for example, thermoelectric) is inserted inside the lower end, although not shown. Pair) is installed. That is, the temperature measuring cylinder 8 is configured to measure the temperature of the bottom side portion inside the outer pipe 3.

Then, as shown in FIG. 1, the operation control unit M supplies the fuel gas to the burner B by the fuel gas supply unit 10 and supplies the combustion air to the burner B. The amount of combustion air by the unit 11 is adjusted to control the amount of combustion of the burner B.
That is, in the operating state in which the operation control unit M generates the reforming gas K, the temperature on the bottom side of the outer pipe 3 is set to the target temperature (for example, 800) based on the measured temperature measured by the temperature measuring cylinder 8. The temperature is maintained at (° C.), so that the fuel gas supply amount by the fuel gas supply unit 10 and the combustion air amount by the air supply unit 11 are adjusted.

Specifically, since the present embodiment includes a plurality of reaction tubes A, the operation control unit M measures the temperature measured by the temperature measurement cylinders 8 provided in each of the plurality of reaction tubes A. In order to maintain the highest temperature among them at the target temperature (for example, 800 ° C.), the temperature control process for adjusting the fuel gas supply amount by the fuel gas supply unit 10 and the combustion air amount by the air supply unit 11 is executed. It is configured to do.

(Details of heat exchanger for steam generation)
As shown in FIG. 1, the steam generation heat exchanger J is configured such that the heat transfer pipes 7 are spirally arranged along the outer periphery of the side wall 2S of the reformer H.
That is, a pure water introduction pipe portion 7a to which pure water W is supplied is formed at the lower end portion of the heat transfer pipe 7, and steam discharge to supply steam to the raw material gas pipe 5 at the upper end portion of the heat transfer pipe 7. The pipe portion 7b is formed.

Therefore, in the steam generation heat exchanger J, the pure water W supplied to the pure water introduction pipe portion 7a is transferred by the heat transfer pipe 7 which is heated by the combustion gas flowing in the external space F. It is configured to generate steam by flowing through the inside of the heat pipe 7, and is configured to supply the generated steam from the steam discharge pipe portion 7b to the raw material gas pipe 5.

(Details of heat exchanger for air preheating)
As shown in FIGS. 1 and 2, the air preheating heat exchanger N is configured to have a cylindrical shape that allows air to flow between the cylindrical inner wall 1n and the cylindrical outer wall 1g.
An air introduction unit 1d for introducing combustion air supplied from the air supply unit 11 is provided at a position on the lower side of the air preheating heat exchanger N.
A plurality of air supply pipes 1K connecting the upper side portion of the air preheating heat exchanger N and the burner B are arranged radially along the periphery of the burner B, and the upper wall 2U of the reformer H has a plurality of air supply pipes 1K. It is provided inside.

Therefore, the air preheating heat exchanger N causes the combustion air supplied to the air introduction unit 1d to flow between the inner wall 1n and the outer wall 1g heated by the combustion gas flowing in the outer space F. It is configured to be heated to a high temperature state, and is configured to supply the combustion air heated to a high temperature to the burner B through the air supply pipe 1K.

Incidentally, although the detailed configuration of the burner B is omitted, the fuel gas supply unit 10 is connected to the burner B in addition to the air supply pipe 1K, and the fuel supplied from the fuel gas supply unit 10 is connected. The gas is configured to be burned with combustion air supplied through the air supply pipe 1K.

The fuel gas supply unit 10 supplies the off-gas from the off-gas tank 21 (see FIG. 4), which will be described later, as the fuel gas, and when the off-gas is insufficient, the raw material gas G is supplied as the fuel gas. .. Therefore, although detailed description is omitted, the fuel gas supply unit 10 is configured to include a supply amount adjusting valve for adjusting the supply amount of the off-gas and the supply amount of the raw material gas G.
Further, the air supply unit 11 supplies air by the air supply machine of the blower blower, and is configured so that the air supply amount can be adjusted by adjusting the output of the air supply machine.

(Overall configuration of hydrogen production equipment)
The hydrogen production apparatus 100 will be described with reference to FIG. Note that FIG. 4 illustrates a state when the hydrogen refining operation is being executed. In the figure, the flow paths through which various gases such as the raw material gas G are flowing are indicated by thick lines, and various gases are shown. The flow paths that do not circulate are indicated by thin lines. Regarding the valves that open and close the flow path, those in the open state are shown in white, and those in the closed state are shown in black. The same applies to FIG. 5 showing the standby operation state.

The hydrogen production apparatus 100 adsorbs and removes impurities contained in the reformer R provided with the reformer H described above and the metamorphic gas supplied from the reformer R to remove impurities, and is a product gas having a high hydrogen concentration. 20 is provided with a pressure fluctuation adsorption type hydrogen separating unit 20 for purifying.
The operation control unit M described above is configured to control the operation of the reforming unit R and the hydrogen separation unit 20.

(Details of reforming part)
The reforming unit R includes a desulfurizer 12 for desulfurizing the raw material gas G pumped by the compressor D, a reformer H for supplying the desulfurized raw material gas G in a mixed state of steam, and a reforming gas. It is provided with a CO modifier 17 that transforms carbon monoxide by reacting it with steam.
A raw material gas valve V1 for interrupting the supply of the raw material gas G and adjusting the supply amount of the raw material gas G is provided at a position on the upper side of the compressor D.

The raw material gas G pumped by the compressor D is supplied to the desulfurizer 12 through the first flow path L1. The desulfurization device 12 is filled with a desulfurization catalyst such as Ni—Mo type or ZnO type, and the desulfurization catalyst is configured to remove sulfur components such as an odorant in the raw material gas G.
The desulfurized raw material gas G is supplied to the reformer H through the second flow path L2 (corresponding to the raw material gas pipe 5 described above). The steam generated by the water vapor generation heat exchanger J is supplied to the second flow path L2, and the water vapor is mixed with the raw material gas G flowing through the second flow path L2.

Then, in the reformer H, as described above, the reaction tube A is heated by the combustion of the burner B, and the raw material gas G mixed with steam is steam reformed to generate the reformed gas K. It is configured as follows.
Note that FIG. 4 schematically shows the configuration of the reformer H, and the description of the air supply unit 11 that supplies combustion air to the burner B is omitted.

The reforming gas K obtained by the reformer H is transferred to the CO transformer 17 that reacts carbon monoxide in the reforming gas with steam through the third flow path L3 (corresponding to the reforming gas pipe 6 described above). Be supplied. The CO metamorphizer 17 is filled with a carbon monoxide transformation catalyst, and carbon monoxide in the reformed gas reacts with steam to be converted into hydrogen and carbon dioxide.
By the reaction in the CO transformer 17, the reformed gas K becomes a modified gas containing hydrogen, carbon monoxide, carbon dioxide and methane (hydrogen concentration is 64 to 96% by volume).
Since the desulfurization reaction in the desulfurization device 12 is an exothermic reaction and the CO transformation reaction in the CO transformation device 17 is an endothermic reaction, they can be exchanged with each other by storing them in an integrated reaction vessel. There is.

(About the flow of metamorphic gas)
The metamorphic gas discharged from the CO metamorphic device 17 exchanges heat with the cooling water by the second heat exchanger 18 while flowing through the fourth flow path L4 to lower the temperature, and the water vapor is liquefied. Moisture is removed by the water vapor, and then the water is guided to the hydrogen separation unit 20 through the fifth flow path L5.
The fifth flow path L5 is provided with a modified gas valve V5 that opens and closes the fifth flow path L5.

The fifth flow path L5 is branched with a return path L10 that bypasses the PSA device 22 and returns the modified gas from which the water has been removed by the gas-liquid separation unit 19 to the upstream side of the compressor D.
The return path L10 is provided with a return valve V10 that opens and closes the return path L10.

Although not shown, a desulfurization return line is provided to return the modified gas from which water has been removed by the gas-liquid separation unit 19 to the upstream side of the compressor D for desulfurization treatment in the desulfurization device 12. And there is a desulfurization on-off valve that opens and closes the desulfurization return line.
The on-off valve for desulfurization treatment will be opened during the hydrogen purification operation described later, and closed at other times.

Further, an exhaust passage L12 for discharging the gas flowing through the fifth flow path L5 to the outside is branched into the fifth flow path L5. The exhaust passage L12 is provided with an exhaust valve V12 that opens and closes the exhaust passage L12.

By the way, using the first flow path L1, the second flow path L2, the third flow path L3, the fourth flow path L4, and the return path L10, the gas that has passed through the CO transformer 17 is transformed into the desulfurizer 12 and the transformer. A closed circulation circuit C that circulates through the pawnbroker H and the CO transformer 17 can be formed (see FIG. 5).
The return path L10 in the closed circulation circuit C is provided with a pressure detecting unit P for detecting the internal pressure in the closed circulation circuit C.

(Details of hydrogen separator)
The hydrogen separation unit 20 is a pressure swing adsorption type PSA device that separates impurities (miscellaneous gases) other than hydrogen from the metamorphic gas transformed by the CO metamorphic device 17 to purify a product gas having a high concentration of hydrogen gas. A 22 is provided, a product tank 23 for storing the purified product gas, and an off-gas tank 21 for storing the off-gas discharged from the PSA device 22.

The PSA device 22 is provided with a plurality of (three in the embodiment) adsorption towers 20a, 20b, and 20c. Each of the adsorption towers 20a, 20b, and 20c is filled with a combination of a zeolite-based adsorbent, activated carbon, silica gel, and the like as an adsorbent.
In each of the adsorption towers 20a, 20b, 20c, the adsorption step, the depressurization step, the purge step, and the step-up step (PSA method process) are executed in the plurality of adsorption towers 20a, 20b, 20c with different phases. It is configured to purify the product gas having a high hydrogen gas concentration.

Although detailed description is omitted, in the above-mentioned process (PSA method process), a plurality of valves (not shown) provided in each flow passage connected to the plurality of suction towers 20a, 20b, 20c by the operation control unit M. ) Is opened and closed, and it is executed sequentially.
Note that FIG. 4 shows a state in which the adsorption tower 20a is undergoing an adsorption step of flowing a metamorphic gas to obtain a product gas.

The product gas purified by the PSA device 22 is supplied to the product tank 23 through the sixth flow path L6, and the product gas stored in the product tank 23 is stably supplied to the hydrogen-using portion.
The sixth flow path L6 is provided with a product gas valve V6 that opens and closes the sixth flow path L6.
The off-gas (miscellaneous gas) after hydrogen is separated by the PSA device 22 is supplied to the off-gas tank 21 through the seventh flow path L7.
The seventh flow path L7 is provided with an off-gas valve V7 that opens and closes the seventh flow path L7.

Since the off-gas stored in the off-gas tank 21 contains flammable gas such as methane and hydrogen, it is guided to the fuel gas supply unit 10 via the off-gas flow passage L8, and is used as fuel gas from the fuel gas supply unit 10 to the burner B. Is supplied to.
The off-gas flow passage L8 is provided with an off-gas return valve V8 that opens and closes the off-gas flow passage L8.
Although FIG. 4 shows only the flow of the product gas, there is a timing in which the delivery of the product gas and the delivery of the off-gas are simultaneously performed for different adsorption towers 20a, 20b, and 20c.

Incidentally, in order to execute the hydrogen purge process described later, a hydrogen supply path L11 for supplying hydrogen gas from the product tank 23 to the return path L10 is provided.
The hydrogen supply path L11 is provided with a hydrogen gas valve V11 that opens and closes the hydrogen supply path L11.

(Details of hydrogen purification operation)
As shown in FIG. 4, in the hydrogen purification operation state, the raw material gas G passes through the raw material gas valve V1 and then is pressure-fed by the compressor D, flows through the first flow path L1 and is guided to the desulfurizer 12. It is desulfurized. After that, the raw material gas G mixed with steam is guided to the reformer H and steam reformed to generate the reformed gas K. The reformed gas K is metamorphosed by the CO transformer 17, the transformed gas is cooled by the second heat exchanger 18, water is removed by the gas-liquid separation unit 19, and then the modified gas K is passed through the fifth flow path L5. It is introduced into the hydrogen separation unit 20 to purify the product gas (hydrogen gas).

(Details of standby operation)
When the hydrogen refining operation is temporarily stopped and the production of hydrogen gas is temporarily stopped, the product gas filled in the closed circulation circuit C while the reformer H is continuously heated by the burner B. A standby operation is executed in which (hydrogen gas) is circulated through the closed circulation circuit C through the compressor D, the desulfurization device 12, the reformer H, and the CO metamorphic device 17 (see FIG. 5).

That is, when shifting from the hydrogen purification operation to the standby operation, first, while continuously operating the compressor D, the mixing (supply) of steam and the heating of the reformer H by the burner B are continuously performed. The raw material gas valve V1, the modified gas valve V5, and the return valve V10 are closed, and the hydrogen gas valve V11 and the exhaust valve V12 are opened to perform a hydrogen purge process for supplying the product gas (hydrogen gas) to the closed circulation circuit C. Will do.
By this hydrogen purging process, the product gas (hydrogen gas) is allowed to flow in the closed circulation circuit C, and the gas remaining in the closed circulation circuit C is discharged from the exhaust passage L12, while the inside of the closed circulation circuit C is filled with the product gas (hydrogen gas). Replace with hydrogen gas).

After that, as shown in FIG. 5, the mixing (supply) of steam is stopped and the hydrogen gas valve is stopped while the compressor D is continuously operated and the reformer H is continuously heated by the burner B. By closing V11 and the exhaust valve V12 and opening the return valve V10, the product gas (hydrogen gas) filled in the closed circulation circuit C is circulated through the closed circulation circuit C in a standby operation. ..
By the way, when the detection pressure of the pressure detection unit P drops below the predetermined pressure during the standby operation, the hydrogen gas valve V11 is opened so as to supply the hydrogen gas from the product tank 23 into the closed circulation circuit C. Therefore, it is configured to be controlled so as to maintain the pressure in the closed circulation circuit C at a predetermined pressure.

Although detailed description is omitted, when the standby operation is executed, the hydrogen substitution treatment of supplying the product gas (hydrogen gas) to the adsorption towers 20a, 20b, 20c of the PSA device 22 and filling the adsorption towers 20a, 20b, 20c is performed. Is done.

When shifting from the standby operation to the hydrogen purification operation, for example, first, the compressor D is continuously operated, and the reformer H is continuously heated by the burner B, and then steam is mixed (supplied). , And the raw material gas valve V1 and the modified gas valve V5 are opened, and the return valve V10 is closed so that the modified gas is supplied to the PSA device 22.
Although detailed description is omitted, after restarting the operation, the PSA device 22 exhausts the purified product gas until the hydrogen concentration of the refined product gas becomes equal to or higher than the set value, and the hydrogen concentration of the purified product gas becomes high. When the value exceeds the set value, the refined product gas is stored in the product tank 23.

(About stop operation)
When the hydrogen purification operation is stopped and the production of hydrogen gas is stopped for a long period of time (for example, longer than several days), the hydrogen purging treatment described above is first performed, and then the compressor D is continued. In the activated state, stop the mixing (supply) of steam, stop the heating of the reformer H by the burner B, open the hydrogen gas valve V11 and the exhaust valve V12, and close the return valve V10. As a result, the product gas (hydrogen gas) filled in the closed circulation circuit C is allowed to flow through the closed circulation circuit C, so that the water vapor discharge process for discharging the water vapor inside the closed circulation circuit C is performed.

After that, the compressor D was stopped, the mixing (supply) of steam was continuously stopped, the heating of the reformer H by the burner B was continuously stopped, and the hydrogen gas valve V11 and the exhaust valve V12 were closed. Therefore, a hydrogen filling process for filling the inside of the closed circulation circuit C with a product gas (hydrogen gas) is performed.
Although detailed description is omitted, when the stop operation is executed, the adsorption towers 20a, 20b, and 20c of the PSA device 22 are filled with the product gas (hydrogen gas) by supplying the product gas (hydrogen gas). Is done.

(About temperature rise operation)
When restarting the operation from the stopped operation state, first, the temperature raising operation is executed. That is, the operation of the compressor D is started with the mixing (supply) of water vapor stopped and the raw material gas valve V1, the modified gas valve V5, the hydrogen gas valve V11 and the exhaust valve V12 closed, and the burner B The heating of the reformer H is started to raise the temperature of the desulfurization device 12, the reformer H, and the CO metamorphic device 17 while flowing the product gas (hydrogen gas) filled through the closed circulation circuit C. ..

After that, when the temperature of the desulfurizer 12, the reformer H, and the CO transformer 17 rises, the mixing (supply) of steam is started, the raw material gas valve V1 and the modified gas valve V5 are opened, and the return valve V10 is closed. Then, the modified gas is supplied to the PSA device 22.
Although detailed description is omitted, after restarting the operation, the PSA device 22 exhausts the purified product gas until the hydrogen concentration of the refined product gas becomes equal to or higher than the set value, and the hydrogen concentration of the purified product gas becomes high. When the value exceeds the set value, the refined product gas is stored in the product tank 23.

(About operation control)
The operation control unit M will execute the above-mentioned temperature control process when performing the hydrogen purification operation.
That is, in order to maintain the highest temperature among the temperatures measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A at the target temperature (for example, 800 ° C.), the fuel gas supply unit. The temperature control process for adjusting the fuel gas supply amount by 10 and the combustion air amount by the air supply unit 11 is executed.

Then, when the operation control unit M performs the hydrogen purification operation, in addition to the temperature control process described above, the operation control unit M lowers the temperature that becomes the highest temperature among the temperatures measured by the temperature measurement cylinder 8, so that heat exchange is performed. It is configured to perform a temperature lowering treatment that increases the bypass flow amount of the reforming gas K for bypass while reducing the heating flow amount of the reforming gas K for bypassing.

Specifically, in the present embodiment, there is a temperature that is higher than the set temperature with respect to the lowest temperature measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A. In this case, the temperature of the reaction tube A, which becomes higher than the set temperature, is increased by increasing the bypass flow amount of the reforming gas K for bypass while reducing the heating flow amount of the reforming gas K for heat exchange. It is configured to reduce.
By the way, when the temperature that becomes the highest temperature among the temperatures measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A decreases, the temperature control process is executed accordingly. ..

Therefore, the supply amount of the raw material gas G supplied to a part of the plurality of reaction tubes A is due to the variation in the branching amount of the raw material gas G branched and supplied to the plurality of reaction tubes A. Even if the temperature measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A varies due to a decrease or the like, the temperature lowering treatment is executed to perform the temperature measuring cylinder 8 It is possible to lower the temperature that becomes a high temperature among the temperatures measured in the above, and the temperature control process is executed accordingly. As a result, the processing amount of the raw material gas G can be increased. ..

Further, the operation control unit M executes a bypass flow process that controls the adjusting unit 6V so that the bypass flow amount becomes larger than the heating flow amount in the above-mentioned temperature rise operation state in which the operation is started from the operation stop state. It is configured in.
Specifically, in the present embodiment, when the temperature raising operation is performed, the processing for increasing the bypass flow amount by setting the heating flow amount to zero is executed.
When executing the bypass flow process, the operation control unit M sets the highest temperature among the temperatures measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A as the target temperature (target temperature). For example, in order to maintain the temperature at 800 ° C.), a temperature control process for adjusting the fuel gas supply amount by the fuel gas supply unit 10 and the combustion air amount by the air supply unit 11 is executed.

If the bypass flow treatment is executed, the amount of bypass flow increases, and the temperature measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A decreases. Since the amount of combustion of the burner B is increased by executing the temperature control process, the time required for the temperature raising operation can be shortened.

(About temperature changes)
Based on FIG. 6, the temperature of each part with the passage of time during the temperature raising operation will be described.
In the above embodiment, the temperature raising operation is performed while flowing the product gas (hydrogen gas) through the closed circulation circuit C, but the experimental result shown in FIG. 6 shows that the raw material gas G is supplied from the start of the operation. It shows the temperature change of each part in the state where steam is mixed and the burner B is burned, and the modified gas from the CO transformer 17 is released to the outside.

In the figure, "reformation temperature-none" means the temperature measurement cylinder 8 in a state where the entire amount of the reforming gas K is allowed to flow through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. The "reform temperature" means the temperature measured in the above, and the "reform temperature" means the temperature measurement cylinder 8 in a state where a part of the reform gas K is flowed through the bypass flow path Qb inside the inner inner pipe 4b. Means the temperature measured.

The "bypass outlet temperature" is the temperature at which the reformed gas K for bypass flowing through the bypass flow path Qb flows into the auxiliary guide pipe 6B.
Further, "reaction tube outlet temperature-none" means that the entire amount of the reforming gas K is used as the reforming gas K for heat exchange and flows through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. The temperature of the reformed gas K after merging flowing through the reformed gas pipe 6 in the state of being allowed to flow, and the “reaction tube outlet temperature” means a part of the reformed gas K inside the inner inner pipe 4b. It means the temperature of the reformed gas K after merging that flows through the reformed gas pipe 6 in a state of being flowed through the bypass flow path Qb.

When the temperature raising operation is started, the temperature measured by the temperature measuring cylinder 8, the outlet temperature of the reformed gas K for bypass, and the temperature of the reformed gas K after merging gradually increase.
Then, in a state where a part of the reforming gas K is made to flow as the reforming gas K for bypass through the bypass flow path Qb, it is made to flow through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. Since the amount of heating flow of the reforming gas K for heat exchange decreases, the "reforming temperature" gradually rises while maintaining a state of being lower than the "reforming temperature-none".

Similarly, in a state where a part of the reforming gas K is made to flow as the reforming gas K for bypass through the bypass flow path Qb, it flows through the heating flow path Qa between the outer inner pipe 4a and the inner inner pipe 4b. By reducing the amount of heating flow of the reforming gas K for heat exchange, the "reaction tube outlet temperature" gradually rises while maintaining a state higher than "reaction tube outlet temperature-none". Become.

Therefore, if the reformed gas K is allowed to flow through the bypass flow path Qb inside the inner inner pipe 4b during the temperature raising operation, the temperature of the reformed gas K flowing through the reformed gas pipe 6 after merging can be adjusted. By raising the temperature, it becomes easy to raise the temperature of the CO transformer 17 and the desulfurizer 12 that exchanges heat with the CO transformer 17, and as a result, the time required for the temperature raising operation can be shortened. ..
Incidentally, as described in the above embodiment, the same applies to the case where the temperature of the desulfurizer 12, the reformer H, and the CO transformer 17 is raised while the product gas (hydrogen gas) filled through the closed circulation circuit C is flowing. be.

Further, when it is necessary to lower the temperature measured by the temperature measuring cylinder 8 when performing the hydrogen purification operation, a part of the reforming gas K is used as a bypass flow path inside the inner inner pipe 4b. If it is allowed to flow through Qb, the flow rate of the reforming gas K for heat exchange flowing through between the outer inner pipe 4a and the inner inner pipe 4b is reduced, and the temperature is measured by the temperature measuring cylinder 8. The temperature can be lowered.

[Another Embodiment]

(1) In the above embodiment, the reformer H (reformer) including a plurality of reaction tubes A has been illustrated, but with respect to the reformer H (reformer) having a single reaction tube A. The present invention is also applicable.
In this case, it can be effectively used to shorten the time required for the temperature raising operation.

(2) In the above embodiment, the case where the reformer H (reformer) includes the steam generation heat exchanger J and the air preheating heat exchanger N is illustrated, but the steam generation heat exchanger J and It may be carried out in the form of forming the reformer H (reformer) without the heat exchanger N for air preheating.

(3) In the above embodiment, the case where the hydrogen filling process for filling the product gas (hydrogen gas) is performed in the stopped operation is illustrated, but instead of the product gas (hydrogen gas), the nitrogen gas filled with nitrogen gas is used. It may be carried out in the form of performing a filling process.

(4) In the above embodiment, the case where the hydrogen separation unit 20 for separating and processing the hydrogen gas is provided for the metamorphic gas from the reforming unit R is illustrated, but the metamorphic gas is supplied to the gas engine as a product gas, etc. , The modified gas may be used as it is.

(5) In the above embodiment, the case where the heating flow amount is set to zero is illustrated in the bypass flow treatment, but the bypass flow amount is set to be larger than the heating flow amount without making the heating flow amount zero. It may be carried out in the form.

(6) In the above embodiment, in the temperature lowering treatment, the temperature becomes higher than the set temperature with respect to the lowest temperature measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A. When the temperature exists, the bypass flow amount of the reforming gas K for bypass is increased while reducing the heating flow amount of the reforming gas K for heat exchange in the reaction tube A which becomes higher than the set temperature. The case of executing the process of lowering the temperature has been illustrated, but the processing form of the temperature lowering process can be changed in various ways.

For example, for the reaction tube A having the highest temperature among the temperatures measured by the temperature measuring cylinders 8 provided in each of the plurality of reaction tubes A, the heating flow amount of the reforming gas K for heat exchange is determined. The temperature measuring cylinder 8 provided in each of the plurality of reaction tubes A by repeating the process of increasing the bypass flow amount of the reforming gas K for bypass and lowering the temperature while decreasing the temperature. The specific form of the temperature lowering process can be changed in various ways, such as keeping the temperature measured in the above within the set range.

(7) In the above embodiment, the case of reforming to a reformed gas having a large amount of hydrogen component has been illustrated, but the present invention can also be applied to the case of reforming to a reformed gas having a large amount of methane component.

The configuration disclosed in the above embodiment (including another embodiment, the same shall apply hereinafter) can be applied in combination with the configuration disclosed in other embodiments as long as there is no contradiction. The embodiments disclosed in the present specification are examples, and the embodiments of the present invention are not limited thereto, and can be appropriately modified without departing from the object of the present invention.

3 Outer pipe 4 Inner pipe 4a Outer inner pipe 4b Inner inner pipe 5 Raw material gas supply part 6V Adjustment part 8 Temperature detection part 12 Desulfurizer 17 CO Transformer A Reaction tube B Combustion part H Reformer M Operation control part Qa For heating Flow path Qb Bypass flow path

Claims (4)

A reaction tube in which an inner tube having an open bottom is arranged inside an outer tube whose bottom is closed, and a filling portion filled with a catalyst is formed in a vertical direction between the outer tube and the inner tube. When,
A raw material gas supply unit that supplies a hydrocarbon-based raw material gas mixed with water vapor to the upper side of the filling unit, and a raw material gas supply unit.
A reformer provided with a combustion unit that heats the outer surface of the outer pipe.
The inner pipe is composed of an outer inner pipe facing the outer pipe and an inner inner pipe arranged inside the outer inner pipe.
A heating flow path is provided between the outer inner pipe and the inner inner pipe to allow the reformed gas discharged from the lower side of the filling portion to flow upward and discharge from the reaction pipe.
Inside the inner inner pipe, a bypass flow path is provided in which the reformed gas discharged from the lower side of the filling portion is allowed to flow upward and discharged from the reaction pipe.
A reformer provided with an adjusting unit for adjusting a heating flow amount for flowing the reformed gas through the heating flow path and a bypass flow amount for flowing the reformed gas through the bypass flow path. A temperature detection unit for detecting the temperature of the bottom side portion inside the reaction tube is provided.
The reformer according to claim 1, wherein the operation control unit executes a temperature control process for controlling the combustion amount of the combustion unit in order to maintain the temperature of the temperature detection unit at the target temperature. A plurality of the reaction tubes are juxtaposed in a state where the raw material gas is branched and supplied.
The temperature at which the operation control unit increases the bypass flow amount for the reaction tube having a high temperature in order to reduce the higher temperature among the temperatures detected by the temperature detection unit in each of the plurality of reaction tubes. A request for executing a lowering process and, as the temperature control process, executing a process of maintaining the highest temperature among the temperatures detected by the temperature detection unit in each of the plurality of reaction tubes at the target temperature. Item 2. The reformer according to Item 2. A reforming processing apparatus including the reformer according to any one of claims 1 to 3.
The raw material gas is a gas desulfurized by a desulfurizer and mixed with steam, and the reformed gas discharged from the reformer is supplied to the CO metamorphic part.
A reforming processing device that executes a bypass flow process that controls the adjusting unit so that the bypass flow amount becomes larger than the heating flow amount in the temperature rise operation state in which the operation control unit starts the operation from the operation stop state. ..

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