JP2003335502A - Hydrogen production apparatus and operation method thereof - Google Patents
Hydrogen production apparatus and operation method thereofInfo
- Publication number
- JP2003335502A JP2003335502A JP2002142403A JP2002142403A JP2003335502A JP 2003335502 A JP2003335502 A JP 2003335502A JP 2002142403 A JP2002142403 A JP 2002142403A JP 2002142403 A JP2002142403 A JP 2002142403A JP 2003335502 A JP2003335502 A JP 2003335502A
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- Prior art keywords
- reformer
- hydrogen
- temperature
- gas
- heating
- Prior art date
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Hydrogen, Water And Hydrids (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
(57)【要約】
【課題】改質器と水素ＰＳＡ装置を備えるものにおい
て、改質器のバーナーのメンテナンスが容易で、構成が
シンプルな水素製造装置を得る。
【解決手段】炭化水素燃料を改質器２において水素リッ
チな改質ガスへと改質し、この改質ガスを水素ＰＳＡ装
置１０に導入して高純度の水素を製造するものにおい
て、改質器２を高温に加熱するためのバーナーに供給す
る燃焼空気を予め昇温用電気ヒーター２０によって高温
に加熱して、改質器２を昇温し、この昇温用電気ヒータ
ー２０の出力を制御することによって改質器２の温度を
所定温度に保持する。
(57) [Problem] To provide a hydrogen production apparatus having a reformer and a hydrogen PSA device, in which a burner of the reformer can be easily maintained and whose configuration is simple. The reformer reforms a hydrocarbon fuel into a hydrogen-rich reformed gas and introduces the reformed gas into a hydrogen PSA apparatus to produce high-purity hydrogen. The combustion air supplied to the burner for heating the reformer 2 to a high temperature is heated in advance to a high temperature by an electric heater 20 for heating, the temperature of the reformer 2 is increased, and the output of the electric heater 20 for heating is controlled. By doing so, the temperature of the reformer 2 is maintained at a predetermined temperature.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、都市ガスやＬＰＧ
等の炭化水素を原燃料とし、水蒸気改質法により水素リ
ッチな改質ガスを生成する改質器とこの改質ガスからＰ
ＳＡ法によって高純度の水素を製造する水素ＰＳＡ装置
とを備えた水素製造装置、およびその運転方法に関す
る。TECHNICAL FIELD The present invention relates to city gas and LPG.
And a reformer that produces a hydrogen-rich reformed gas by a steam reforming method using hydrocarbons such as
The present invention relates to a hydrogen production apparatus including a hydrogen PSA apparatus that produces high-purity hydrogen by the SA method, and an operating method thereof.
【０００２】[0002]
【従来の技術】図２は、従来のこの種の水素製造装置の
システム系統図である。本水素製造装置は、図に見られ
るように、水蒸気改質法によって炭化水素燃料を水素リ
ッチな改質ガスへと改質する改質器２と、改質器２で得
られた改質ガスからＰＳＡ（Pressure swing adsorptio
n ）法によって高純度の水素を製造する水素ＰＳＡ装置
１０とを備えて構成されている。なお、図において、１
は、改質器２の加熱用バーナーに燃焼空気を供給する空
気ブロア、３は、原燃料を脱硫する脱硫器、４は、改質
器２で得られた改質ガス中の一酸化炭素を水素と二酸化
炭素とに変えるＣＯ変成器、５は、水蒸気改質に用いら
れる水蒸気を得る水蒸気分離器、６は、脱硫後の原燃料
に水蒸気分離器５より送られた水蒸気を混合させるスチ
ームエジェクタである。また、７は排熱回収器、８は冷
却水循環ポンプ、９は改質ガス圧縮機である。本構成の
水素製造装置に原燃料として炭化水素燃料を供給する
と、炭化水素燃料は改質器２において水蒸気改質され、
改質器出口ガスライン（Ａ）のドライガスの組成は、例
えば、水素 75 ％、二酸化炭素 11 ％、一酸化炭素 11
％、メタン3％となる。上記の組成のガスはＣＯ変成器
３に送られ、一酸化炭素が水素と二酸化炭素とに変成さ
れて、ＣＯ変成器出口ガスライン（Ｂ）のドライガスの
組成は、例えば、水素 77 ％、二酸化炭素 20 ％、メタ
ン 3％となる。次に、この組成よりなる改質ガスは、改
質ガス圧縮機９により昇圧され、水素ＰＳＡ装置１０へ
と供給される。水素ＰＳＡ装置１０では、改質ガス中の
水素のみが選択的にピックアップされ、水素純度が 99.
99％以上のガスが製品水素として製造される。なお、水
素ＰＳＡ装置１０で製品水素として得られる水素の量
は、改質ガス中の水素の 80 ％程度であり、残余の水素
は、二酸化炭素およびメタンとともに、水素ＰＳＡ装置
オフガスライン（Ｃ）を経て改質器２の加熱用バーナー
へと送られて燃焼され、その燃焼熱が、改質器２での水
蒸気改質反応（吸熱反応）に必要な熱に利用されてい
る。2. Description of the Related Art FIG. 2 is a system diagram of a conventional hydrogen producing apparatus of this type. As shown in the figure, the present hydrogen production apparatus includes a reformer 2 for reforming a hydrocarbon fuel into a hydrogen-rich reformed gas by a steam reforming method, and a reformed gas obtained by the reformer 2. To PSA (Pressure swing adsorptio
The hydrogen PSA apparatus 10 for producing high-purity hydrogen by the n) method. In the figure, 1
Is an air blower for supplying combustion air to the heating burner of the reformer 2, 3 is a desulfurizer for desulfurizing raw fuel, 4 is carbon monoxide in the reformed gas obtained in the reformer 2. A CO shifter for converting hydrogen and carbon dioxide, 5 is a steam separator for obtaining steam used for steam reforming, and 6 is a steam ejector for mixing the steam sent from the steam separator 5 with the desulfurized raw fuel. Is. Further, 7 is an exhaust heat recovery device, 8 is a cooling water circulation pump, and 9 is a reformed gas compressor. When a hydrocarbon fuel is supplied as a raw fuel to the hydrogen production apparatus of this configuration, the hydrocarbon fuel is steam reformed in the reformer 2,
The composition of the dry gas at the reformer outlet gas line (A) is, for example, 75% hydrogen, 11% carbon dioxide, 11 carbon monoxide.
% And methane 3%. The gas having the above composition is sent to the CO shift converter 3, carbon monoxide is transformed into hydrogen and carbon dioxide, and the dry gas composition of the CO shift outlet gas line (B) is, for example, 77% hydrogen. Carbon dioxide is 20% and methane is 3%. Next, the reformed gas having this composition is pressurized by the reformed gas compressor 9 and supplied to the hydrogen PSA device 10. In the hydrogen PSA device 10, only hydrogen in the reformed gas is selectively picked up, and the hydrogen purity is 99.
Over 99% of the gas is produced as product hydrogen. The amount of hydrogen obtained as product hydrogen in the hydrogen PSA device 10 is about 80% of the hydrogen in the reformed gas, and the remaining hydrogen flows through the hydrogen PSA device off-gas line (C) together with carbon dioxide and methane. After that, it is sent to the heating burner of the reformer 2 and burned, and the heat of combustion is used as the heat required for the steam reforming reaction (endothermic reaction) in the reformer 2.
【０００３】[0003]
【発明が解決しようとする課題】上記のごとき水素製造
装置の改質器２においては、水蒸気改質反応が700 ℃程
度の高温で行われるため、装置の起動時には改質器２を
この温度に昇温する必要がある。このため、従来の装置
では、起動時には弁１１を調節し、原燃料の一部を改質
器２の加熱用バーナーへと送って燃焼させることにより
改質器２を昇温している。一方、定常運転時には、既に
述べたように、水素ＰＳＡ装置１０で得られた残余の水
素を同一の加熱用バーナーへと送って燃焼させ、所定温
度に保持している。したがって、改質器２の加熱用バー
ナーはこれらの２種類の燃焼に対応する役割を担ってい
る。In the reformer 2 of the hydrogen producing apparatus as described above, since the steam reforming reaction is carried out at a high temperature of about 700 ° C., the reformer 2 is kept at this temperature when the apparatus is started. It is necessary to raise the temperature. Therefore, in the conventional apparatus, the valve 11 is adjusted at the time of start-up, and a part of the raw fuel is sent to the heating burner of the reformer 2 and burned to raise the temperature of the reformer 2. On the other hand, during the steady operation, as described above, the residual hydrogen obtained by the hydrogen PSA apparatus 10 is sent to the same heating burner to be burned and kept at a predetermined temperature. Therefore, the heating burner of the reformer 2 plays a role corresponding to these two types of combustion.
【０００４】このとき、起動時に燃焼される原燃料、例
えば天然ガスの単位体積当たりの発熱量は約 36000 kJ/
Nm3 であるのに対して、定常運転時に燃焼される水素Ｐ
ＳＡ装置１０のオフガスの単位体積当たりの発熱量は約
7000 kJ/Nm3であり、５倍以上の違いがある。さらに、
定常運転時の所要燃焼量は起動時の所要燃焼量の６倍以
上であるので、加熱用バーナーへ供給される燃料流量
比、すなわち、定常運転時の燃料流量と起動時の燃料流
量との比は 30 以上となる。At this time, the calorific value per unit volume of the raw fuel burned at the time of start-up, for example natural gas, is about 36000 kJ /
Whereas a Nm 3, hydrogen is burned during normal operation P
The calorific value per unit volume of the off gas of the SA device 10 is about
It is 7,000 kJ / Nm 3, which is more than 5 times the difference. further,
Since the required combustion amount during steady operation is 6 times or more than the required combustion amount during startup, the fuel flow rate ratio supplied to the heating burner, that is, the ratio of the fuel flow rate during steady operation and the fuel flow rate during startup Is over 30.
【０００５】しかるに、このように流量に大きな違いの
ある二つの燃料を、単一の加熱用バーナーで、かついず
れも安定に燃焼させることは困難であり、従来の装置に
おいては、原燃料を燃焼させる起動時に安定した燃焼が
得られず、加熱用バーナーにカーボンが析出し、析出し
たカーボンが蓄積して加熱用バーナーの着火が不調にな
るという不具合があり、定期的に加熱用バーナーのクリ
ーニングを実施しなければならないという問題点があ
る。However, it is difficult to stably burn two fuels having such a large difference in flow rate with a single heating burner, and in the conventional device, the raw fuel is burned. There is a problem that stable combustion cannot be obtained at the time of starting, carbon deposits on the heating burner, and the deposited carbon accumulates and the ignition of the heating burner becomes improper, so cleaning the heating burner regularly There is a problem that it must be implemented.
【０００６】また、改質器２で安定に水素を生成するた
めには、改質器２の温度を適正な温度に保持する必要が
ある。この改質器２の温度は、吸熱である改質反応熱量
と発熱である加熱用バーナーの燃焼熱量とのバランスに
より決まり、改質反応熱量は原燃料の流量に比例し、加
熱用バーナーの燃焼熱量は水素ＰＳＡ装置１０のオフガ
ス流量に比例する。これらの流量のうち原燃料の流量
は、必要とする製品水素の量により設定されるので、従
来の装置においては、図２に示した水素ＰＳＡ装置オフ
ガスライン（Ｃ）の分岐回路に設けた弁１２を制御し、
加熱用バーナーに送る水素ＰＳＡ装置１０のオフガス流
量を調節して発熱量を調整することによって、改質器２
の温度を適正な温度に保持する方法が採られている。ま
た、水素ＰＳＡ装置１０における水素の収率、すなわ
ち、投入される水素量に対する製品水素として取出され
る水素量の割合は、水素ＰＳＡ装置１０の運転状態によ
って数％変動するため、予め多めの改質ガスを供給して
水素の収率の変動に対処するよう配慮されており、余剰
となったオフガスは弁１２を介して外部に放出されてい
る。Further, in order to stably generate hydrogen in the reformer 2, it is necessary to maintain the temperature of the reformer 2 at an appropriate temperature. The temperature of the reformer 2 is determined by the balance between the heat of reforming reaction which is endothermic and the heat of combustion of the heating burner which is exothermic. The heat of reforming reaction is proportional to the flow rate of the raw fuel and the combustion of the heating burner. The amount of heat is proportional to the off gas flow rate of the hydrogen PSA device 10. Among these flow rates, the flow rate of the raw fuel is set according to the required amount of product hydrogen. Therefore, in the conventional apparatus, the valve provided in the branch circuit of the hydrogen PSA apparatus off-gas line (C) shown in FIG. Control twelve,
By adjusting the off-gas flow rate of the hydrogen PSA apparatus 10 sent to the heating burner to adjust the calorific value, the reformer 2
The method of keeping the temperature of the above at an appropriate temperature is adopted. Further, the yield of hydrogen in the hydrogen PSA apparatus 10, that is, the ratio of the amount of hydrogen taken out as product hydrogen to the amount of hydrogen charged varies by several% depending on the operating state of the hydrogen PSA apparatus 10, so a large amount of advance is required. It is considered that the quality gas is supplied to cope with the fluctuation of the yield of hydrogen, and the excess off-gas is released to the outside through the valve 12.
【０００７】しかしながら、このように水素ＰＳＡ装置
オフガスライン（Ｃ）に分岐回路を設け、加熱用バーナ
ーに送るオフガス量を調節し、余剰となったオフガスを
外部に放出する構成においては、分岐回路より放出され
るオフガスが可燃性ガスであり、そのまま大気中に放出
することはできないので、図示しない処理装置を付設す
る必要がある。このため、コストが高く、かつ所要設置
スペースが大きくなるという問題点があった。However, in such a configuration in which the hydrogen PSA apparatus off-gas line (C) is provided with a branch circuit, the amount of off-gas sent to the heating burner is adjusted, and the excess off-gas is discharged to the outside, Since the off gas released is a combustible gas and cannot be released into the atmosphere as it is, it is necessary to attach a processing device (not shown). Therefore, there are problems that the cost is high and the required installation space is large.
【０００８】本発明は上記のごとき従来技術の現状を考
慮してなされたもので、本発明の目的は、改質器と水素
ＰＳＡ装置とを備えるものにおいて、改質器の加熱バー
ナーへのカーボン蓄積に依る不具合が回避され、さらに
は、従来用いられていた余剰オフガス用の処理装置の設
置が不要となり、メンテナンスが容易で、コストが廉
く、かつコンパクトな構成の改質器を備えた水素製造装
置と、その運転方法を提供することにある。The present invention has been made in view of the current state of the art as described above, and an object of the present invention is to provide a reformer and a hydrogen PSA device with carbon for a heating burner of the reformer. In addition to avoiding problems due to accumulation, there is no need to install a treatment device for surplus off-gas that was used in the past, maintenance is easy, cost is low, and a hydrogen reformer with a compact structure is provided. It is to provide a manufacturing apparatus and an operating method thereof.
【０００９】[0009]
【課題を解決するための手段】上記の目的を達成するた
めに、本発明においては、（１）水蒸気改質法によって
炭化水素燃料を水素リッチな改質ガスへと改質する改質
器と、この改質器で得られた前記の改質ガスからＰＳＡ
法によって高純度の水素を製造する水素ＰＳＡ装置とを
備えた水素製造装置において、上記の改質器の加熱用バ
ーナーに供給する燃焼空気の供給系統に、この燃焼空気
を予め加熱して供給するための加熱手段として電気ヒー
ターを備えることとする。In order to achieve the above object, in the present invention, (1) a reformer for reforming a hydrocarbon fuel into a hydrogen-rich reformed gas by a steam reforming method. , PSA from the reformed gas obtained in this reformer
In a hydrogen production apparatus provided with a hydrogen PSA apparatus for producing high-purity hydrogen by a method, this combustion air is preheated and supplied to a combustion air supply system to be supplied to a heating burner of the reformer. An electric heater is provided as a heating means for this.
【００１０】また、上記（１）の水素製造装置を運転す
る際、（２）改質器の昇温時に、改質器の加熱用バーナ
ーに供給する燃焼空気の温度を、加熱手段を用いて 200
℃以上に予熱して供給することとする。（３）また、改
質器の定常運転時に、改質器特性温度、例えば、加熱用
バーナーの火炎の温度、若しくはこの火炎の温度に対応
して変化する改質器の構成部材の温度等の改質器特性温
度の検出信号によって加熱手段の出力を調整し、改質器
特性温度を規定値に保持して運転することとする。Further, when the hydrogen producing apparatus of (1) is operated, (2) when the temperature of the reformer is raised, the temperature of the combustion air supplied to the heating burner of the reformer is adjusted by using a heating means. 200
It shall be supplied after being preheated to ℃ or above. (3) Further, during steady operation of the reformer, the characteristic temperature of the reformer, for example, the temperature of the flame of the heating burner, or the temperature of the components of the reformer that changes corresponding to the temperature of the flame, etc. The output of the heating means is adjusted by the detection signal of the reformer characteristic temperature, and the reformer characteristic temperature is maintained at a specified value for operation.
【００１１】この種の水素製造装置においては、既に述
べたように、改質器の昇温時には天然ガス等の原燃料と
燃焼空気とを加熱用バーナーで燃焼させることにより昇
温が行われ、定常運転時には水素ＰＳＡ装置のオフガス
とを加熱用バーナーで燃焼させることにより改質器が所
定の温度に保持されている。この加熱用バーナーでの燃
焼速度は、燃焼前のガスの温度と相関があり、燃焼前の
ガスの温度が高いほど燃焼速度が大きくなる。したがっ
て、上記の（１）のごとく、加熱用バーナーに供給する
燃焼空気の供給系統に、この燃焼空気を予め加熱して供
給するための加熱手段を備えることとすれば、加熱用バ
ーナーへ供給するガス流量を変えなくとも、加熱手段を
調節することによって加熱用バーナーでの燃焼速度、し
たがって発熱量を制御することができることとなる。In the hydrogen producing apparatus of this type, as mentioned above, when the temperature of the reformer is raised, the temperature is raised by burning the raw fuel such as natural gas and the combustion air with the heating burner. During steady operation, the reformer is maintained at a predetermined temperature by burning off gas of the hydrogen PSA unit with a heating burner. The burning rate in the heating burner has a correlation with the temperature of the gas before burning, and the burning rate increases as the temperature of the gas before burning rises. Therefore, as in the above (1), if the supply system of the combustion air to be supplied to the heating burner is provided with a heating means for preheating and supplying this combustion air, it is supplied to the heating burner. Even if the gas flow rate is not changed, it is possible to control the combustion rate in the heating burner and thus the calorific value by adjusting the heating means.
【００１２】改質器の昇温時に供給される天然ガスの主
成分であるメタンと空気との燃焼速度は、燃焼前のガス
温度が 300℃のとき、常温のガスの場合の約 5倍とな
り、効果的に昇温できる。また、燃焼前のガス温度が 2
00℃以上であれば、カーボンの析出が微小に抑えられ
る。したがって、上記の（２）のごとく運転することと
すれば、カーボンの析出が微小に抑えられ、メンテナン
スの所要頻度が大幅に低下するので効率的に運転するこ
とが可能となる。また、上記のように、加熱手段を調節
することによって加熱用バーナーでの燃焼速度、したが
って発熱量を制御することができるので、上記の（３）
のごとく、定常運転の際、改質器特性温度の検出信号に
よって加熱手段の出力を調整し、改質器特性温度を規定
値に保持して運転することとすれば、水素の収率等の変
動により水素ＰＳＡ装置のオフガスの流量が変動して
も、燃焼温度を所定値に保持して改質器の温度を適正に
制御することができるので、従来の装置のように水素Ｐ
ＳＡ装置のオフガスの流量に余裕を持たせる必要はな
く、余剰のオフガスを放出する必要もない。したがっ
て、余剰のオフガス用の処理装置も不要となり、コンパ
クトで、低コストの装置が得られることとなる。When the temperature of the gas before combustion is 300 ° C., the burning rate of methane, which is the main component of natural gas supplied when the temperature of the reformer rises, is about 5 times that of the gas at room temperature. The temperature can be raised effectively. Also, the gas temperature before combustion is 2
If the temperature is 00 ° C or higher, the precipitation of carbon can be suppressed minutely. Therefore, if the operation is performed as in the above (2), the precipitation of carbon is suppressed to a minute level, and the required frequency of maintenance is significantly reduced, so that the operation can be efficiently performed. Further, as described above, by adjusting the heating means, it is possible to control the combustion speed in the heating burner, and thus the calorific value.
As described above, during steady operation, the output of the heating means is adjusted by the detection signal of the reformer characteristic temperature, and if the reformer characteristic temperature is maintained at the specified value, the hydrogen yield, etc. Even if the flow rate of the off gas of the hydrogen PSA apparatus fluctuates due to fluctuations, the combustion temperature can be maintained at a predetermined value and the temperature of the reformer can be appropriately controlled.
It is not necessary to allow the flow rate of the off gas of the SA device to have a margin, and it is not necessary to discharge the excess off gas. Therefore, a treatment device for excess off-gas is not required, and a compact and low-cost device can be obtained.
【００１３】[0013]
【発明の実施の形態】図１は、本発明の水素製造装置の
実施例のシステム系統図である。本システム系統図に示
された構成要素のうち、図２の従来のシステム系統図の
構成要素と同一機能を有する構成要素には同一符号を付
して、重複する説明は省略する。本実施例の構成と従来
例の構成との相違点は、第一に、本実施例の構成におい
ては、改質器２の加熱用バーナーへ燃焼用空気を供給す
る燃焼用空気ライン（Ａ）に、燃焼用空気を加熱する加
熱手段としての昇温用電気ヒーター２０が備えられてい
ることにある。また第二の相違点は、従来の構成におい
て水素ＰＳＡ装置オフガスライン（Ｃ）に設けられてい
た余剰オフガス放出用の分岐回路が、本実施例の構成に
は備えられていないことにある。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 is a system diagram of an embodiment of the hydrogen production apparatus of the present invention. Of the components shown in this system diagram, the components having the same functions as those of the conventional system diagram in FIG. 2 are designated by the same reference numerals, and the duplicate description will be omitted. The difference between the configuration of the present embodiment and the configuration of the conventional example is, firstly, in the configuration of the present embodiment, a combustion air line (A) that supplies combustion air to the heating burner of the reformer 2. In addition, the electric heater 20 for raising the temperature is provided as a heating means for heating the combustion air. The second difference is that the branch circuit for discharging excess off-gas, which is provided in the hydrogen PSA device off-gas line (C) in the conventional configuration, is not provided in the configuration of this embodiment.
【００１４】したがって、本実施例の構成の水素製造装
置では、改質器２の加熱用バーナーへ供給する燃焼用空
気の温度を制御し、これによって燃焼速度を調節するこ
とができる。例えば、改質器２の昇温時に、昇温用電気
ヒーター２０によって燃焼空気の温度を 200℃以上に上
げて加熱用バーナーへと供給すれば、カーボンの析出が
微小に抑えられるので、クリーニングの所要頻度が大幅
に低減し、メンテナンスが容易となる。また、定常運転
時に、水素の収率が変動し、水素ＰＳＡ装置のオフガス
流量が変動しても、昇温用電気ヒーター２０によって燃
焼空気の予熱温度を調節して加熱用バーナーの燃焼温度
を制御できるので、例えば、加熱用バーナーの火炎温度
等の改質器特性温度を検出し、この温度が規定値となる
ように昇温用電気ヒーター２０の出力を制御することに
よって、改質器の温度を適正値に保持することができ
る。したがって、改質器の温度の制御に際して水素ＰＳ
Ａ装置のオフガス量を制御する必要はなく、従来の装置
に組み込まれていた余剰ガス放出用の分岐回路を設置す
る必要はなく、放出ガスの処理装置も不要となる。Therefore, in the hydrogen producing apparatus of the present embodiment, the temperature of the combustion air supplied to the heating burner of the reformer 2 can be controlled, and the combustion speed can be adjusted accordingly. For example, when the temperature of the reformer 2 is raised, if the temperature of the combustion air is raised to 200 ° C. or higher by the electric heater 20 for temperature rise and supplied to the heating burner, the precipitation of carbon can be suppressed minutely, so that The required frequency is greatly reduced and maintenance is easy. Further, even when the hydrogen yield fluctuates and the off-gas flow rate of the hydrogen PSA device fluctuates during steady operation, the preheating temperature of the combustion air is adjusted by the temperature raising electric heater 20 to control the combustion temperature of the heating burner. Therefore, the temperature of the reformer can be controlled by, for example, detecting the reformer characteristic temperature such as the flame temperature of the heating burner and controlling the output of the temperature raising electric heater 20 so that this temperature becomes a specified value. Can be held at an appropriate value. Therefore, when controlling the temperature of the reformer, hydrogen PS
It is not necessary to control the off-gas amount of the device A, it is not necessary to install a branch circuit for discharging the surplus gas that is incorporated in the conventional device, and a device for processing the discharged gas is not required.
【００１５】[0015]
【発明の効果】以上述べたように、本発明によれば、
（１）水蒸気改質法によって炭化水素燃料を水素リッチ
な改質ガスへと改質する改質器と、この改質器で得られ
た前記の改質ガスから ＰＳＡ法によって高純度の水素
を製造する水素ＰＳＡ装置とを備えた水素製造装置を請
求項１に記載のごとく構成したので、改質器の加熱用バ
ーナーへのカーボンの析出が極めて小さく抑えられ、か
つ水素ＰＳＡ装置からのオフガスの処理装置が不要とな
ったので、メンテナンスが容易で、コストが廉く、かつ
コンパクトな構成の改質器を備えた水素製造装置が得ら
れることとなった。As described above, according to the present invention, (1) a reformer for reforming a hydrocarbon fuel into a hydrogen-rich reformed gas by a steam reforming method, and this reformer A hydrogen production apparatus comprising a hydrogen PSA apparatus for producing high-purity hydrogen from the obtained reformed gas by the PSA method is configured as described in claim 1, so that the heating burner of the reformer is supplied with the hydrogen production apparatus. Since the precipitation of carbon is suppressed to a very small level and the off-gas processing device from the hydrogen PSA device is not required, maintenance is easy, the cost is low, and the hydrogen production device is equipped with a compact reformer. Will be obtained.
【００１６】（２）また、この水素製造装置は、請求項
２、あるいは請求項３，４のごとく運転すれば、効果的
にしようすることができる。(2) Further, this hydrogen producing apparatus can be effectively used if it is operated as claimed in claim 2 or claim 3 or 4.
【図１】本発明の水素製造装置の実施例のシステム系統
図FIG. 1 is a system diagram of an embodiment of a hydrogen production device of the present invention.
【図２】従来のこの種の水素製造装置のシステム系統図FIG. 2 is a system diagram of a conventional hydrogen production device of this type.
１ 空気ブロア ２ 改質器 ３ 脱硫器 ４ ＣＯ変成器 ５ 水蒸気分離器 ６ スチームエジェクタ ９ 改質ガス圧縮機 １０ 水素ＰＳＡ装置 ２０ 昇温用電気ヒーター 1 air blower 2 reformer 3 desulfurizer 4 CO transformer 5 Water vapor separator 6 steam ejector 9 reformed gas compressor 10 Hydrogen PSA equipment 20 Electric heater for heating
Claims (4)
リッチな改質ガスへと改質する改質器と、該改質器で得
られた前記の改質ガスからＰＳＡ法によって高純度の水
素を製造する水素ＰＳＡ装置とを備えた水素製造装置に
おいて、 前記改質器の加熱用バーナーに供給する燃焼空気の供給
系統に、該燃焼空気を予め加熱して供給するための加熱
手段として電気ヒーターが備えられていることを特徴と
する水素製造装置。1. A reformer for reforming a hydrocarbon fuel into a hydrogen-rich reformed gas by a steam reforming method, and a high-purity reformer obtained by the reformer by the PSA method. In a hydrogen production apparatus comprising a hydrogen PSA apparatus for producing hydrogen, an electric device is provided as a heating means for preheating and supplying the combustion air to a supply system of the combustion air to be supplied to the heating burner of the reformer. A hydrogen production device characterized by being equipped with a heater.
ナーに供給する燃焼空気の温度を、前記加熱手段を用い
て 200℃以上に予熱して供給することを特徴とする請求
項１に記載の水素製造装置の運転方法。2. When the temperature of the reformer is raised, the temperature of the combustion air supplied to the heating burner of the reformer is preheated to 200 ° C. or higher by using the heating means and supplied. The method for operating the hydrogen generator according to claim 1.
検出信号によって前記加熱手段の出力を調整し、改質器
特性温度を規定値に保持して運転することを特徴とする
請求項１に記載の水素製造装置の運転方法。3. When the reformer is in a steady operation, the output of the heating means is adjusted by the detection signal of the reformer characteristic temperature, and the reformer characteristic temperature is maintained at a specified value for operation. The method for operating the hydrogen generator according to claim 1.
において、前記の改質器特性温度が、該改質器の加熱用
バーナーの火炎の温度、若しくはこの火炎の温度に対応
して変化する改質器の構成部材の温度であることを特徴
とする水素製造装置の運転方法。4. The method of operating a hydrogen generator according to claim 3, wherein the reformer characteristic temperature corresponds to a flame temperature of a heating burner of the reformer or a temperature of the flame. A method for operating a hydrogen generator, wherein the temperature of the constituent members of the reformer changes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002142403A JP2003335502A (en) | 2002-05-17 | 2002-05-17 | Hydrogen production apparatus and operation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002142403A JP2003335502A (en) | 2002-05-17 | 2002-05-17 | Hydrogen production apparatus and operation method thereof |
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| Publication Number | Publication Date |
|---|---|
| JP2003335502A true JP2003335502A (en) | 2003-11-25 |
Family
ID=29702694
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2002142403A Withdrawn JP2003335502A (en) | 2002-05-17 | 2002-05-17 | Hydrogen production apparatus and operation method thereof |
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| Country | Link |
|---|---|
| JP (1) | JP2003335502A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006006479A1 (en) * | 2004-07-12 | 2006-01-19 | Sumitomo Seika Chemicals Co., Ltd. | Hydrogen production system and reforming apparatus |
| JP2007070130A (en) * | 2005-09-05 | 2007-03-22 | Fuji Electric Holdings Co Ltd | Hydrogen generator and power generation system provided with the same |
| WO2013061513A1 (en) * | 2011-10-24 | 2013-05-02 | パナソニック株式会社 | Fuel cell system and method for operating same |
-
2002
- 2002-05-17 JP JP2002142403A patent/JP2003335502A/en not_active Withdrawn
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006006479A1 (en) * | 2004-07-12 | 2006-01-19 | Sumitomo Seika Chemicals Co., Ltd. | Hydrogen production system and reforming apparatus |
| AU2005261096B2 (en) * | 2004-07-12 | 2010-01-21 | Sumitomo Seika Chemicals Co., Ltd. | Hydrogen production system and reforming apparatus |
| KR101162255B1 (en) | 2004-07-12 | 2012-07-03 | 스미토모 세이카 가부시키가이샤 | Hydrogen production system and reforming apparatus |
| US8690972B2 (en) | 2004-07-12 | 2014-04-08 | Sumitomo Seika Chemicals Co., Ltd. | Hydrogen production system and reforming apparatus |
| JP2007070130A (en) * | 2005-09-05 | 2007-03-22 | Fuji Electric Holdings Co Ltd | Hydrogen generator and power generation system provided with the same |
| WO2013061513A1 (en) * | 2011-10-24 | 2013-05-02 | パナソニック株式会社 | Fuel cell system and method for operating same |
| JP5236844B1 (en) * | 2011-10-24 | 2013-07-17 | パナソニック株式会社 | Fuel cell system and operation method thereof |
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