JP2007112654A - Method for starting reformer, and reformer - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To start an autoxidative and internally-heatable reformer without using a preheater. <P>SOLUTION: The method for starting the autoxidative and internally-heatable reformer 1 which has an outside preliminary reforming chamber 2 having a reforming catalyst layer 4 and an inside main reforming chamber 3 having a mixed catalyst layer 5 where a reforming catalyst and an oxidation catalyst are mixed, comprises the steps of: heating the outside of the preliminary reforming chamber 2 by a heating means 30 before starting the reformer 1 to keep the mixed catalyst layer 5 at the oxidation reaction temperature by transferring the heat from the preliminary reforming chamber; and heating the outside of the preliminary reforming chamber 2 by the heating means 30 when starting the reformer 1 to raise the temperature of the mixed catalyst layer 5 to the oxidation reaction temperature by transferring the heat from the preliminary reforming chamber and start the autoxidative and internally-heatable reformer. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a method of starting a self-oxidation internal heating type reformer having a mixed catalyst layer in which a steam reforming catalyst and an oxidation catalyst are mixed, and the reformer.

2. Description of the Related Art Conventionally, a reformer that generates a hydrogen-rich reformed gas by steam reforming a mixture of a source gas and steam (hereinafter referred to as a source-steam mixture) in the presence of a reforming catalyst is known.
The hydrogen-rich reformed gas obtained in the reformer is further converted into CO ₂ by reacting a small amount of CO (carbon monoxide) contained therein with an oxygen-containing gas in the presence of a catalyst by means of CO reduction means, In particular, solid polymer electrolyte fuel cells and the like that operate at low temperatures are suitably used as fuel for fuel cells after reducing CO to several ppm level. As the source gas, hydrocarbons such as methane, aliphatic alcohols such as methanol, ethers such as dimethyl ether, city gas, and the like are used. In the reformer, the reaction formula of steam reforming when methane is used as a raw material gas can be expressed as CH ₄ + 2H ₂ O → CO ₂ + 4H ₂ , and the preferred reforming reaction temperature is 650 to 750 ° C. It is a range.

  There are an external heating type and an internal heating type as a system for supplying heat necessary for the reforming reaction of the steam reformer. The external heating type reforming apparatus is an apparatus that generates a reformed gas by providing a heating unit outside and reacting a raw material gas and water vapor with a heat source. The internal heating type reformer is provided with a partial oxidation reaction layer on the supply side (upstream side), and the steam reforming reaction layer disposed on the downstream side using the heat generated in the partial oxidation reaction layer is subjected to a steam reforming reaction. This is an apparatus for heating to a temperature and generating a hydrogen-rich reformed gas by performing a steam reforming reaction with the heated steam reforming catalyst layer.

The partial oxidation reaction can be represented by CH ₄ + 1/2 · O ₂ → CO + 2H ₂ , and the preferable partial oxidation reaction temperature is in the range of 250 ° C. or higher. For example, Patent Documents 1 and 2 describe a self-oxidation internal heating type reformer as an improvement of the internal heating type reforming apparatus. The reformers of Patent Documents 1 and 2 are provided with a so-called pre-reformation chamber and a main reforming chamber, and the pre-reforming chamber is provided with a feed part of the raw material-steam mixture, a reforming catalyst layer and a discharge part. The quality chamber is provided with a supply portion for receiving the effluent from the discharge portion, an oxygen-containing gas supply portion, a mixed catalyst layer in which the reforming catalyst and the oxidation catalyst are mixed, a shift catalyst layer, and a reforming gas discharge portion. Yes.

  FIG. 3 is a sectional view schematically showing an example of a conventionally known auto-oxidation internal heating type reformer. The reformer 1 includes an outer preliminary reforming chamber 2 and an inner main reforming chamber 3 arranged in a double cylinder shape, and a reforming catalyst layer 4 is provided in the preliminary reforming chamber 2. Further, a mixed catalyst layer 5 and a shift catalyst layer 6 in which a reforming catalyst and an oxidation catalyst are mixed are provided. The shift catalyst layer 6 includes a high temperature shift catalyst layer 7 and a low temperature shift catalyst layer 8.

The reforming catalyst is a steam reforming of the raw material gas. For example, a Ni-based reforming reaction catalyst such as NiO—A1 ₂ O or NiO—SiO ₂ .A1 ₂ O ₃ or WO ₂ —SiO ₂ .A1 ₂ O ₃ NiO-W0 ₂ · SiO ₂ · A1 ₂ O ₃ or the like is used. The reforming catalyst constituting the mixed catalyst layer 5 is the same as described above, and the oxidation catalyst uniformly dispersed therein is the temperature required for the steam reforming reaction by causing the source gas in the source-steam mixture to oxidize and generate heat. For example, platinum (Pt), rhodium (Rh), ruthenium (Ru), or palladium (Pd) is used. The mixing ratio of the oxidation catalyst to the reforming catalyst is selected in the range of about 1 to 15% according to the type of the raw material gas to be steam reformed. For example, when methane is used as the raw material gas, it is about 5% ± 2%. In the case of methanol, the mixing ratio is about 2% ± 1%.

  A raw material-steam mixture supply unit 9 is provided in the lower part of the preliminary reforming chamber 2, and a discharge unit 10 for discharging the effluent after the preliminary reforming is provided in the upper part. A supply unit 11 communicating with the discharge unit 10 of the preliminary reforming chamber 2 is provided in the upper part of the main reforming chamber 3, and a reformed gas discharge unit 12 is provided in the lower part. Further, a preheater 13 is connected to the upper portion of the main reforming chamber 3, and a supply pipe 14 for supplying an oxygen-containing gas such as air is extended to the central portion of the main reforming chamber 3. The preheater 13 rapidly raises the mixed catalyst layer 5 to the oxidation reaction temperature when the system is started up. An electric heater is disposed inside the preheater 13 and an oxidation catalyst such as platinum (Pt) or palladium (Pd) is provided. Filled.

  A water vapor from a water vapor generating means (not shown), a raw material gas from a raw material supply section, an oxygen-containing gas (start air) from an oxygen-containing gas supply means, and the like can be introduced into the fluid introduction section of the suction mixing means 15 constituted by an ejector. It is like that. In the illustrated example, a start air pipe provided with a flow rate adjusting valve 16 in the fluid introduction section, a steam pipe from a steam generation means (not shown), and a source gas pipe from a source gas supply section (not shown) are connected. Is done.

  The discharge part of the suction mixing means 15 is communicated with the pre-heater 13 via a pipe 18 provided with a flow rate adjusting valve 17 and also connected to the supply part of the preliminary reforming chamber 2 via a pipe 20 provided with a flow rate adjusting valve 19. Communicated. A heating unit 21 composed of an electric heater is provided below the preliminary reforming chamber 2, and the shift catalyst layer 6 is kept at, for example, about 200 ° C. by heat transfer from the heating unit 21 during the stop period of the reformer 1. To prevent condensation.

  When starting up the self-oxidation internal heating type reformer, it is necessary to first raise the temperature of the mixed catalyst layer 5 to the oxidation reaction temperature. For this reason, when the reformer 1 is started, first, the operation of a steam generation means (not shown) is started, and the heat retention of the shift catalyst layer 6 by the heating unit 21 is stopped. Further, the oxidation catalyst in the preheater 13 is heated to a predetermined temperature by an electric heater. When the oxidation catalyst of the preheater 13 reaches a temperature at which the oxidation reaction can be performed, the flow rate adjusting valves 16 and 17 are opened, and the mixed fluid of starting air and source gas is supplied from the suction mixing means 15 to the preheater 13 through the pipe 18. Supply. In addition, while water vapor | steam is not supplied, source gas can be pressurized with a pump and it can supply to the suction mixing means 15, for example.

  The raw material gas and the starting air supplied to the preheater 13 react (combust) with a part of the raw material gas with oxygen contained in the starting air in the presence of the oxidation catalyst. The mixed catalyst layer 3 is heated with the high temperature gas. When the water vapor generated at the predetermined pressure is generated by the water vapor generating means, the water vapor is supplied to the mixing and sucking means 15. At the same time, when the source gas supply is switched from the pressurized pump line to the bypass line, the source gas is efficiently sucked into the suction mixing means 15 by the suction force of the steam, and the mixed fluid of the source-steam mixture and the start air is discharged from the discharge part. It flows out and is supplied to the preheater 13.

  The flow rate of the mixed fluid of the raw material-steam mixture and the start air can be adjusted by increasing or decreasing the steam flow rate by a flow rate adjusting valve (not shown) provided in the steam supply pipe, but normally the temperature of the mixed catalyst layer 5 is accelerated. Therefore, the flow rate of the raw material gas and the starting air is adjusted to be increased before the water vapor is not supplied to the mixed suction means 13. When the source gas and the starting air whose flow rate is increased are supplied to the preheater 13, the heat of oxidation due to the oxidation reaction is increased and the heating rate of the mixed catalyst layer 3 is also accelerated. A part of the raw material gas not burned by the preheater 13 flows into the mixed catalyst layer 3 as the remaining raw material gas.

  When the mixed catalyst layer 3 reaches the oxidation reaction temperature, when an oxygen-containing gas for operation (oxidation air) is supplied from the supply pipe 14, the remaining raw material gas supplied from the preheater 13 is oxidized air. The mixed catalyst layer 3 is further heated by the oxidation heat. Next, when the mixed catalyst layer 3 reaches the reforming reaction temperature, the flow rate adjusting valve 19 is opened, and the raw material-steam mixture is supplied from the suction mixing means 15 to the preliminary reforming chamber 2. Next, the supply of the starting air to the suction mixing means 15 is stopped, and the flow rate adjusting valve 17 is closed to stop the operation of the preheater 13. Thereafter, the normal operation state is gradually entered when each part of the reformer 1 reaches the operation temperature.

JP 2001-192201 A JP-A-2005-149860

  In the conventional starting method, it is necessary to install a pre-heater, and a pipe switching means for starting-operation switching is also required. In addition, it is necessary to monitor the temperature of the pre-heater, and there is a problem that the system becomes complicated and the cost increases. Accordingly, an object of the present invention is to solve the problems in such a conventional self-oxidation internal heating type reformer, and an object thereof is to provide a new reformer start-up method and a reformer.

The method for starting the reformer of the present invention that solves the above-described problem is a method for starting a self-oxidation internal heating type reformer having a mixed catalyst layer in which a reforming catalyst and an oxidation catalyst are mixed.
The reformer has an outer pre-reforming chamber provided with a reforming catalyst layer and an inner main reforming chamber provided with a mixed catalyst layer, and the outer side of the pre-reforming chamber before starting the reformer. Is heated by heating means, and the mixed catalyst layer is kept at the oxidation reaction temperature by heat transfer, or the outside of the preliminary reforming chamber is heated by heating means at the time of starting the reformer, and the heat transfer The mixed catalyst layer is started by raising the temperature to an oxidation reaction temperature.
And the said heating means can be comprised with an electric heater (Claims 1, 2).

Another starting method of the reformer of the present invention that solves the above problem is a method of starting a self-oxidation internal heating type reformer having a mixed catalyst layer in which a reforming catalyst and an oxidation catalyst are mixed.
The reformer has an outer pre-reforming chamber provided with a reforming catalyst layer and an inner main reforming chamber provided with a mixed catalyst layer, and the mixed catalyst layer is placed in the main reforming chamber before starting the reformer. The oxidation reaction temperature is kept at the oxidation reaction temperature by radiant heat from the heating means provided above the reforming chamber, or the mixed catalyst layer is radiated heat from the heating means provided above the main reforming chamber when starting the reformer. It is characterized in that it is started by raising the temperature to
And the said heating means can be comprised with an electric heater (Claims 3 and 4).

The reformer of the present invention that solves the above problems is a self-oxidation internal heating type reformer having a mixed catalyst layer in which a reforming catalyst and an oxidation catalyst are mixed,
The reformer has an outer pre-reforming chamber provided with a reforming catalyst layer and an inner main reforming chamber provided with a mixed catalyst layer, and the mixed catalyst layer is transferred to the outside of the pre-reforming chamber. The heating means for heating to the oxidation reaction temperature is provided, or the heating means for heating the mixed catalyst layer to the oxidation reaction temperature by radiant heat is provided above the main reforming chamber.
And the said heating means can be comprised with an electric heater (Claim 5, 6).

  The method for starting the reformer according to claim 1, wherein the outside of the preliminary reforming chamber is heated by a heating means before starting the reformer, and the mixed catalyst layer is kept at the oxidation reaction temperature by the heat transfer, or When the reformer is started, the outside of the preliminary reforming chamber is heated by a heating means, and the mixed catalyst layer is heated to the oxidation reaction temperature by the heat transfer and started. Therefore, it is not necessary to install a preheater as in the conventional start-up method, and there is no need to switch the preheater or monitor the temperature. Furthermore, the system configuration is simplified and lightened, and the installation cost and operation cost can be reduced.

  According to another method of starting the reformer according to claim 3, the mixed catalyst layer is kept at the oxidation reaction temperature by radiant heat from a heating means provided above the main reforming chamber, or the mixed catalyst is started when the reformer is started. It is characterized by starting by raising the temperature to the oxidation reaction temperature by radiant heat from a heating means provided above the main reforming chamber. Therefore, it is not necessary to install a preheater as in the conventional start-up method, and there is no need to switch the preheater or monitor the temperature. In addition, the system configuration is simplified and lightened, and the installation cost and operation cost can be reduced. Furthermore, since the mixed catalyst layer is directly heated by radiant heat, less heat energy is required to keep the mixed catalyst warm or raise its temperature.

  The reformer according to claim 5 is provided with a heating means for heating the mixed catalyst layer to an oxidation reaction temperature by heat transfer outside the preliminary reforming chamber, or the mixed catalyst layer above the main reforming chamber. Since the heating means for heating to the oxidation reaction temperature by radiant heat is provided, there is no need to install a pre-heater like a conventional reformer, the system configuration is simplified, the weight is reduced, and the installation cost is reduced. Operating costs can also be reduced.

  Next, the best embodiment of the reformer of the present invention and the starting method thereof will be described with reference to the drawings. FIG. 1 is a cross-sectional view schematically showing a self-oxidation internal heating type reformer of the present invention. The same parts as those of the conventional reformer of FIG. 3 described above are denoted by the same reference numerals, and redundant description of the structure and operation is omitted as much as possible.

  The embodiment of FIG. 1 differs from the example of FIG. 3 in that a heating means 30 for heating the mixed catalyst layer 5 by heat transfer is provided outside the pre-reforming chamber 2, and instead a preheater 13 and its switching means are provided. The other points are the same. In the present embodiment, an electric heater is used as the heating means 30, but a heating pipe to which a high-temperature combustion gas by burner combustion is supplied may be used. In the example of FIG. 1, the electric heater is attached by a method of winding around the outer preliminary reforming chamber 2.

  Next, a method for starting the reformer 1 of FIG. 1 will be described. As in the conventional method, the lower part of the outer preliminary reforming chamber 2 is heated by the heating unit 21 made of an electric heater during the stop period of the reformer 1, and the shift catalyst layer 6 is about 200 ° C., for example, by the heat transfer. To keep warm. On the other hand, the mixed catalyst layer 5 is kept warm by the heating means 30 at an oxidation reaction temperature (for example, about 260 ° C. when butane or a gas containing butane is used as a raw material gas).

  For example, in the case of a reformer that supplies a fuel cell with hydrogen-rich reformed gas as a fuel, the reformer 1 often repeats operation and stop periodically. The temperature of the mixed catalyst layer 5 at the end of the operation is a reforming temperature which is a high temperature, but if it is left as it is while the reformer 1 is stopped, it gradually cools and falls below the oxidation reaction temperature. Therefore, as described above, the mixed catalyst layer 5 is kept warm by the heating means 30 so as not to be equal to or lower than the oxidation reaction temperature. However, when an electric heater is used as the heating means 30, the power consumption of the mixed catalyst layer 5 is Not much is required because it is sufficient to supply the heat energy required for heat insulation. The temperature of the shift catalyst layer 6 and the mixed catalyst layer 5 is detected by a temperature sensor such as a thermistor or a thermocouple (not shown), and the temperature signal is used for temperature monitoring or temperature control by a control device (not shown).

  In this embodiment, in order to prevent high temperature heat of the mixed catalyst layer 5 from diffusing to the surroundings during operation of the reformer 1, the heat insulating layer 3 a is provided on the outer peripheral surface of the side wall of the main reforming chamber 3 surrounding the mixed catalyst layer 5. Even if such a heat insulating layer 3a is provided, if the heating by the heating means 30 is continued while the reformer 1 is stopped, the heat is transferred to the preliminary reforming chamber 2, and the heat transfer is performed. As a result, the temperature difference between the pre-reforming chamber 2 and the main reforming chamber 3 is reduced, and thermal diffusion from the mixed catalyst layer 5 is suppressed. At the same time, the heat transfer to the pre-reforming chamber 2 is transferred to the mixed catalyst layer 5 by the convection action in the upper space of the reforming catalyst 4, and the temperature can be maintained at the oxidation reaction temperature. If the heat insulating wall 3 a is not provided, the heat of the heating means 30 is more efficiently transferred to the mixed catalyst layer 5.

  When the reformer 1 is started, first, a steam generation means (not shown) is started, and the heat retention of the shift catalyst layer 6 by the heating unit 21 and the heat retention of the mixed catalyst layer 5 by the heating means 30 are stopped. Next, the raw material gas pressurized by the pump is introduced into the suction mixing means 15, and the raw material gas is supplied from the supply unit 9 to the mixed catalyst layer 5 through the preliminary reforming chamber 2. When the mixed catalyst layer 5 is filled with the raw material gas, an oxygen-containing gas (oxidation air) is supplied from the supply pipe 14 to start the oxidation reaction (combustion) of the mixed catalyst layer 5.

  When the oxidation reaction starts, the temperature of the mixed catalyst layer 5 gradually increases due to the oxidation heat. However, when the temperature approaches the temperature at which carbon deposition occurs (for example, near 400 ° C.), the supply of the raw material gas is restricted, and the mixed catalyst layer 5 Control is made so that the temperature does not become higher than that, and the generation of water vapor is awaited. The temperature maintenance of the mixed catalyst layer 5 can be automatically controlled by, for example, a control device (for example, constituted by a computer device) not shown.

  When the water vapor generating means reaches a state where it can generate water vapor of a predetermined pressure, the water vapor is supplied to the suction mixing means 15 to switch the raw material gas to the suction system and the flow rate is increased, and the oxidizing air is supplied from the supply pipe 14. The temperature of the mixed catalyst layer 5 is accelerated by supplying the mixed catalyst layer 5. Note that the flow rate of the source gas and the oxidizing air need to be supplied in a predetermined proportional relationship, but the supply amount can be automatically controlled by the control device. Then, the mixed catalyst layer 5 becomes operable by these operations, and thereafter, the temperature of each part of the reformer 1 is gradually raised to the operating temperature and the normal operation is started.

  In the above description, the heating means 30 is operated while the reformer 1 is stopped to keep the mixed catalyst layer 5 at the oxidation reaction temperature. However, when the heat insulating wall 3a is not provided as described above, It is also possible to start the operation of the heating means 30 at the start of the reformer 1 and raise the temperature of the mixed catalyst layer 5 to the oxidation reaction temperature. In that case, the heating means 30 is stopped when the mixed catalyst layer 5 reaches the oxidation reaction temperature, and thereafter, the starting operation is performed in the same procedure as in the case of the heat retention method.

  FIG. 2 is a sectional view schematically showing another reformer of the self-oxidation internal heating type of the present invention. The same parts as those of the conventional reformer of FIG. 3 or the reformer of FIG. 1 are denoted by the same reference numerals, and redundant description of the structure and operation is omitted as much as possible.

  The embodiment of FIG. 2 differs from the example of FIG. 1 in that it is mixed above the main reforming chamber 3 instead of providing the heating means 30 for heating the mixed catalyst layer 5 by heat transfer outside the pre-reforming chamber 2. The other features are the same, except that a heating means 31 for heating the catalyst layer 5 with radiant heat and a supply section 32 for supplying start air are provided. In the present embodiment, the heating means 31 is constituted by an electric heater, but it may be a heating pipe to which a high-temperature combustion gas by burner combustion is supplied. The electric heater is attached to the upper outside or inside of the main reforming chamber 3.

  Next, the starting method of the reformer 1 of FIG. 2 is demonstrated. Similarly to the conventional method, while the reformer 1 is stopped, the lower part of the outer preliminary reforming chamber 2 is heated by the heating unit 21, and the shift catalyst layer 6 is kept at, for example, about 200 ° C. by the heat transfer. In the present embodiment, first, a water vapor generating means (not shown) is activated, the heat retention of the heating unit 21 is stopped, and the heating means 31 is activated. Since the radiant heat from above by the heating means 31 directly heats the upper surface of the mixed catalyst 5, the temperature of the upper layer portion of the mixed catalyst 5 reaches the oxidation reaction temperature more quickly.

  After at least the upper layer portion of the mixed catalyst layer 5 reaches the oxidation reaction temperature, when the water vapor generating means reaches a state where it can generate water vapor of a predetermined pressure, the water vapor is supplied to the suction mixing means 15. When water vapor is supplied to the suction mixing means 15, the raw material gas is sucked and mixed, and the raw material-water vapor mixture is supplied to the supply unit 9 of the preliminary reforming chamber 2. The raw material-steam mixture reaches the mixed catalyst layer 5 in the main reforming chamber 3 via the preliminary reforming chamber 2. When the start air is supplied from the supply unit 32 when the mixed catalyst layer 5 is filled with the raw material-steam mixture, the oxidation reaction starts mainly in the upper layer portion of the mixed catalyst layer 5 that has reached the oxidation reaction temperature.

  When the oxidation reaction in the upper layer portion of the mixed catalyst layer 5 is started, the oxidation heat diffuses throughout the mixed catalyst layer 5, and the lower layer portion is also gradually heated to the oxidation reaction temperature. When the entire mixed catalyst layer 5 reaches the oxidation reaction temperature, the starting air is stopped and the oxidizing air is supplied from the supply pipe, and the temperature of the mixed catalyst layer 5 is raised to raise the reformer 1. Transition to the operating state.

  The start-up method of the reformer 1 of FIG. 2 described so far is a method of starting the heating means 31 when the reformer 1 is started, and the mixed catalyst layer 5 is subjected to the oxidation reaction temperature while the reformer 1 is stopped. Alternatively, the method may be started by keeping warm. In that case, when the reformer 1 is stopped, the temperature of the mixed catalyst layer 5 that was at the reforming temperature at the time of stopping gradually decreases, and when it reaches the oxidation reaction temperature, a control device (not shown) sends a heating signal to the heating means 31. Is output, and the mixed catalyst layer 5 enters the heat retaining operation. When the upper surface of the mixed catalyst layer 5 is irradiated with the radiant heat of the heating means 31 while the reformer 1 is stopped, the temperature of the upper layer heated by the radiant heat is transferred to the lower layer, and as a result, the entire mixed catalyst layer 5 is The temperature is kept at about the oxidation reaction temperature.

  The starting method when the mixed catalyst layer 5 is kept warm while the reformer 1 is stopped will be described. First, when the reformer 1 is started, a steam generating means (not shown) is started and the heating means 31 is used. The heat retention of the mixed catalyst layer 5 is stopped. Next, when the supply of water vapor from the water vapor generating means becomes possible, when the water vapor is supplied to the suction mixing means 15, the raw material-steam mixture is supplied from the suction mixing means 15 through the preliminary reforming chamber 2. Then, it is supplied to the mixed catalyst layer 5 in the main reforming chamber 3.

  When the air for oxidation is supplied from the supply pipe 14 when the mixed catalyst layer 5 is filled with the raw material-steam mixture, the mixed catalyst layer 5 that has reached the oxidation reaction temperature starts an oxidation reaction. Then, the mixed catalyst layer 5 is further heated by the oxidation heat, and the reformer 1 is gradually shifted to the operating state. In the case of adopting the heat retaining method, it is not necessary to use start air, so the supply unit 32 shown in FIG. 2 is not necessary.

  The reformer and the start-up method of the present invention can be used for a self-oxidation internal heating type reformer.

Sectional drawing which shows typically an example of the conventional self-oxidation internal heating type reformer. Sectional drawing which shows typically the auto-oxidation internal heating type reformer of this invention. Sectional drawing which shows typically the self-oxidation internal heating type other reformer of this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Reformer 2 Preliminary reforming chamber 3 Main reforming chamber 3a Heat insulation wall 4 Reforming catalyst layer 5 Mixed catalyst layer 6 Shift catalyst layer 7 High temperature shift catalyst layer 8 Low temperature shift catalyst layer 9 Supply unit 10 Discharge unit 11 Supply unit 12 Discharge unit 13 Preheater 14 Supply pipe 15 Suction mixing means 16, 17 Flow rate adjustment valve 18 Pipe 19 Flow rate adjustment valve 20 Pipe 21 Heating part 30, 31 Heating means 32 Supply part

Claims (6)

In a method of starting a self-oxidation internal heating type reformer 1 having a mixed catalyst layer 5 in which a reforming catalyst and an oxidation catalyst are mixed,
The reformer 1 has an outer preliminary reforming chamber 2 provided with a reforming catalyst layer 4 and an inner main reforming chamber 3 provided with a mixed catalyst layer 5. The outside of the preliminary reforming chamber 2 is heated by the heating means 30 and the mixed catalyst layer 5 is kept at the oxidation reaction temperature by the heat transfer, or when the reformer 1 is started, the outside of the preliminary reforming chamber 2 is A starting method of a reformer, characterized in that it is heated by a heating means 30 and the mixed catalyst layer 5 is heated to an oxidation reaction temperature by the heat transfer and started.   The reformer start-up method according to claim 1, wherein the heating means (30) comprises an electric heater. In a method of starting a self-oxidation internal heating type reformer 1 having a mixed catalyst layer 5 in which a reforming catalyst and an oxidation catalyst are mixed,
The reformer 1 has an outer preliminary reforming chamber 2 provided with a reforming catalyst layer 4 and an inner main reforming chamber 3 provided with a mixed catalyst layer 5. The mixed catalyst layer 5 is kept at the oxidation reaction temperature by radiant heat from the heating means 31 provided above the main reforming chamber 3, or when the reformer 1 is started, the mixed catalyst layer 5 is kept in the main reforming chamber 3. A reformer start-up method, wherein the start-up is performed by raising the temperature to an oxidation reaction temperature by radiant heat from a heating means 31 provided above.   4. A reformer start-up method according to claim 3, wherein said heating means (31) comprises an electric heater. In the self-oxidation internal heating type reformer 1 having the mixed catalyst layer 5 in which the reforming catalyst and the oxidation catalyst are mixed,
The reformer 1 has an outer preliminary reforming chamber 2 provided with a reforming catalyst layer 3 and an inner main reforming chamber 3 provided with a mixed catalyst layer 5. A heating means 30 for heating the mixed catalyst layer 5 to the oxidation reaction temperature by heat transfer is provided, or a heating means 31 for heating the mixed catalyst layer 5 to the oxidation reaction temperature by radiation heat is provided above the main reforming chamber 3. A reformer characterized by that.   6. The reformer according to claim 5, wherein the heating means 30 or the heating means 31 is composed of an electric heater.

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