JP2005047770A

JP2005047770A - Heat exchanger for reformer

Info

Publication number: JP2005047770A
Application number: JP2003283563A
Authority: JP
Inventors: Katsunori Uchimura; 克則内村; Kokichi Doi; 孝吉土井; Naoto Kagami; 直人各務
Original assignee: Toyota Motor Corp
Current assignee: Toyota Motor Corp
Priority date: 2003-07-31
Filing date: 2003-07-31
Publication date: 2005-02-24

Abstract

PROBLEM TO BE SOLVED: To provide a heat exchanger for a reformer that (a) accelerates the endothermic reforming reaction at the proximity of the entrance part of a reforming gas and that (b) prevents the temperature elevation of the reforming gas at the exit part of the reforming gas in a heat exchanger accompanied by the endothermic reaction. SOLUTION: (1) The heat exchanger for the reformer is a heat exchanger 10 for the reformer accompanied by the endothermic reaction, which forms a plurality of heat exchanging parts 13 with high temperature heat mediums at the passage of the reforming gas and supplies the high temperature heat mediums in parallel to each the heat exchanging part. (2) The heat exchanging part is a laminate type heat exchanger. COPYRIGHT: (C)2005,JPO&NCIPI

Description

本発明は、吸熱反応を伴う改質器用熱交換器に関する。 The present invention relates to a heat exchanger for a reformer with an endothermic reaction.

熱交換器において、熱交換する２流体の温度差を高くとって熱交換効率を上げるために、熱交換する２流体を対向する向きに流すことは知られている（たとえば、特開昭５９−２９９９２号公報）。
本出願人が従来開発してきた、炭化水素系燃料と改質水を含む改質原料から水素リッチの改質ガスを生成する改質器用熱交換器３０においても、図５〜図７に示すように、熱交換効率を高くするために、改質原料、改質ガス（以下、単に「改質ガス」という）の流れ３１と高温熱媒体である燃焼ガスの流れ３２とを、互いに対向する流れとしていた。図５は、図７の積層型熱交換器におけるＣ−Ｃ断面での改質ガス流路を示しており、図６は、図７のＤ−Ｄ断面における燃焼ガス流路を示しており、改質ガスは高温燃焼ガスからの熱を吸熱しながら、水素生成の改質反応を行う。
ＣＨ₄＋Ｈ₂Ｏ → ＣＯ＋３Ｈ₂−Ｑ
ここで、Ｑ：吸熱改質反応の吸熱量
特開昭５９−２９９９２号公報 In a heat exchanger, in order to increase the temperature difference between the two fluids that exchange heat and increase the heat exchange efficiency, it is known that the two fluids that exchange heat flow in opposite directions (for example, Japanese Patent Laid-Open No. Sho 59-59). 29992).
As shown in FIGS. 5 to 7, the heat exchanger 30 for reformer that has been conventionally developed by the present applicant and generates a hydrogen-rich reformed gas from a reformed raw material containing a hydrocarbon-based fuel and reformed water is also shown in FIGS. In addition, in order to increase the heat exchange efficiency, a flow 31 of reforming raw material and reformed gas (hereinafter simply referred to as “reformed gas”) and a flow 32 of combustion gas that is a high-temperature heat medium are opposed to each other. I was trying. FIG. 5 shows the reformed gas flow path in the CC cross section in the stacked heat exchanger of FIG. 7, and FIG. 6 shows the combustion gas flow path in the DD cross section of FIG. The reformed gas performs a reforming reaction for hydrogen generation while absorbing heat from the high-temperature combustion gas.
CH ₄ + H ₂ O → CO + 3H ₂ −Q
Where Q: endothermic amount of the endothermic reforming reaction
JP 59-29992 A

しかし、図５〜図７の改質用熱交換器３０には、つぎの問題点があった。図８は、図５〜図７の改質用熱交換器３０における、改質ガスと燃焼ガスの温度変化を示す。
（イ）図６、図８に示すように、燃焼ガス温度は、燃焼ガス入口部Ａから燃焼ガス出口部Ｂに流れるにしたがい、改質ガスとの熱交換により、大幅に低下する。したがって、改質ガス入口部Ｆ近傍（改質原料が触媒活性温度に上昇し吸熱改質反応の一定温度領域に入った直後の領域）では、改質ガスと燃焼ガスの温度差が小で熱交換されにくく、熱伝達律速になっており、改質ガスにもっと熱を与えて改質反応速度を上げてもよいのにかかわらず、改質ガスへの熱の供給が不足して、改質反応が遅くなっている状態にある。
（ロ）改質ガス出口部Ｅ近傍においては、反応律速になっているにかわらず、燃焼ガス温度が高く維持されて過剰の熱が改質ガスに与えられるため、本来反応に使われるべき熱が、改質ガスの温度上昇に多く使われてしまい（図８のハッチ領域が、燃焼ガスの熱量が改質ガス温度上昇に用いられた部分）、燃焼ガスの熱の改質反応への利用効率が悪くなり、かつ、吸熱改質反応の一定温度領域が狭くなる（一定温度領域に入った後早くから改質ガスの温度が上がるため）。また、改質ガス出口部Ｅにおいて改質ガス温度が高くなり過ぎているため、熱交換器の耐久性が低下する。 However, the reforming heat exchanger 30 of FIGS. 5 to 7 has the following problems. FIG. 8 shows temperature changes of the reformed gas and the combustion gas in the reforming heat exchanger 30 of FIGS.
(A) As shown in FIGS. 6 and 8, the combustion gas temperature greatly decreases due to heat exchange with the reformed gas as it flows from the combustion gas inlet A to the combustion gas outlet B. Therefore, in the vicinity of the reformed gas inlet F (region immediately after the reforming raw material rises to the catalyst activation temperature and enters the constant temperature region of the endothermic reforming reaction), the temperature difference between the reformed gas and the combustion gas is small and heat is reduced. It is difficult to exchange and heat transfer rate-limiting, and even though it is possible to increase the reforming reaction rate by giving more heat to the reformed gas, the supply of heat to the reformed gas is insufficient and reforming The reaction is slow.
(B) In the vicinity of the reformed gas outlet E, the combustion gas temperature is maintained high and excessive heat is given to the reformed gas regardless of the reaction rate limiting, so heat that should be originally used for the reaction However, it is often used to raise the temperature of the reformed gas (the hatched area in FIG. 8 is the part where the amount of heat of the combustion gas is used to raise the temperature of the reformed gas), and the heat of the combustion gas is used for the reforming reaction. The efficiency deteriorates, and the constant temperature region of the endothermic reforming reaction becomes narrow (because the temperature of the reformed gas rises soon after entering the constant temperature region). In addition, since the reformed gas temperature is too high at the reformed gas outlet E, the durability of the heat exchanger decreases.

本発明の目的は、吸熱反応を伴う熱交換器において、
（イ）改質ガス入口部近傍（活性化後の吸熱改質反応の一定温度領域における改質ガス入口に近い領域部分）での燃焼ガス温度を上げ改質ガスへの熱伝達量を増やし従来の熱伝達律速を解消して吸熱改質反応を促進させ、
（ロ）吸熱改質反応の一定温度領域を改質ガス出口側に拡げて改質反応領域を増大させるとともに、改質ガス出口部における改質ガスの温度上昇を抑えた、
改質器用熱交換器を提供することにある。 An object of the present invention is to provide a heat exchanger with an endothermic reaction,
(A) Conventionally, the combustion gas temperature near the reformed gas inlet (the region near the reformed gas inlet in the constant temperature region of the endothermic reforming reaction after activation) is increased to increase the amount of heat transfer to the reformed gas. To eliminate the heat transfer rate limiting of
(B) The constant temperature region of the endothermic reforming reaction is expanded to the reformed gas outlet side to increase the reforming reaction region, and the temperature rise of the reformed gas at the reformed gas outlet is suppressed.
The object is to provide a heat exchanger for a reformer.

上記課題を解決する本発明は、また、上記目的を達成する本発明は、つぎのとおりである。
（１）吸熱反応を伴う改質器用熱交換器であって、改質ガスの流路に対して、高温熱媒体との熱交換部を複数箇所形成し、各熱交換部に対して、高温熱媒体が並列に供給される改質器用熱交換器。
（２）前記熱交換部は、積層型熱交換器である（１）記載の改質器用熱交換器。 The present invention for solving the above-mentioned problems and the present invention for achieving the above object are as follows.
(1) A heat exchanger for a reformer with an endothermic reaction, in which a plurality of heat exchange portions with a high-temperature heat medium are formed in the reformed gas flow path, A heat exchanger for a reformer to which a heating medium is supplied in parallel.
(2) The heat exchanger for a reformer according to (1), wherein the heat exchange unit is a stacked heat exchanger.

上記（１）の改質器用熱交換器によれば、改質ガスの流路に対して、高温熱媒体（燃焼ガス）との熱交換部が、複数箇所、互いに直列に形成され、各熱交換部に高温熱媒体が並列に供給されるので、
（イ）各熱交換部で改質ガスと高温熱媒体との熱交換が行われ、改質ガス入口部近傍での改質原料と高温熱媒体との温度差が大きくなり、改質ガス入口部近傍での高温熱媒体から改質原料への伝達熱量が増え、改質ガス入口部近傍での改質ガスへの熱の供給不足および改質ガス入口部近傍の熱伝達律速が解消され、吸熱改質反応が促進される。
（ロ）また、複数の熱交換部の各熱交換部において吸熱改質反応が促進されることにより、吸熱改質反応の一定温度領域が拡大し（改質ガス出口側に拡大し）、その結果、高温熱媒体の熱量の改質反応への利用量が増えるとともに、改質原料の出口部近傍での改質ガスの温度上昇に使われる熱量が低減する。また、改質ガスの出口部近傍での改質ガスの温度の上昇抑制によって、熱交換器の耐久性も向上する。
上記（２）の改質器用熱交換器によれば、熱交換部が積層型熱交換器であるため、熱交換器がコンパクトになる。 According to the heat exchanger for reformer of (1) above, a plurality of heat exchanging portions with the high-temperature heat medium (combustion gas) are formed in series with each other with respect to the reformed gas flow path. Since a high-temperature heat medium is supplied in parallel to the exchange unit,
(A) The heat exchange between the reformed gas and the high-temperature heat medium is performed in each heat exchange section, and the temperature difference between the reforming raw material and the high-temperature heat medium near the reformed gas inlet section increases, and the reformed gas inlet The amount of heat transferred from the high-temperature heat medium in the vicinity of the reformer to the reforming raw material is increased, the shortage of heat supply to the reformed gas in the vicinity of the reformed gas inlet and the heat transfer rate limiting in the vicinity of the reformed gas inlet are eliminated, The endothermic reforming reaction is promoted.
(B) Further, the endothermic reforming reaction is promoted in each heat exchanging section of the plurality of heat exchanging sections, so that the constant temperature region of the endothermic reforming reaction is expanded (expanded to the reformed gas outlet side). As a result, the amount of heat of the high-temperature heat medium used for the reforming reaction increases, and the amount of heat used to raise the temperature of the reformed gas near the outlet of the reforming raw material decreases. In addition, the durability of the heat exchanger is also improved by suppressing the temperature rise of the reformed gas in the vicinity of the reformed gas outlet.
According to the heat exchanger for reformer of (2) above, the heat exchanger is compact because the heat exchanging part is a stacked heat exchanger.

以下に、本発明の改質器用熱交換器を、図１〜図４を参照して説明する。
本発明の改質器用熱交換器１０は、吸熱反応を伴う反応型の熱交換器である。
改質器用熱交換器１０は、改質原料（炭化水素系燃料、たとえば、メタン、メタノール等と、改質水）を、高温熱媒体（「燃焼ガス」ともいう）との熱交換と、改質触媒により促進された吸熱改質反応を伴って、水素リッチの「改質ガス」を生成する。以下、「改質ガス」という用語には、改質前の「改質原料」も含むものとする。
改質器用熱交換器１０は、改質ガス流路１１と燃焼ガス流路１２を有し、改質ガス流路１１の、伝熱フィンを含む内表面に、改質反応のための改質触媒（貴金属、ニッケル等）が担持されている。改質触媒は、流路壁面への担持に換えて、流路にペレットを配置したものでもよい。
改質ガス流路１１には改質ガス（改質原料であるを含む）が流れ、燃焼ガス流路１２には燃焼ガスが流れる。改質ガスと燃焼ガスは互いに混じり合わない。改質ガス流路１１を流れる改質ガスの流れと、燃焼ガス流路１２を流れる燃焼ガスの流れとは、互いに対向する流れである。 Below, the heat exchanger for reformers of this invention is demonstrated with reference to FIGS.
The heat exchanger for reformer 10 of the present invention is a reaction type heat exchanger that involves an endothermic reaction.
The heat exchanger 10 for reformer is used for heat exchange between reforming raw materials (hydrocarbon fuels such as methane, methanol, etc. and reforming water) with a high-temperature heat medium (also referred to as “combustion gas”). A hydrogen-rich “reformed gas” is produced with an endothermic reforming reaction promoted by a porous catalyst. Hereinafter, the term “reformed gas” includes “reformed raw material” before reforming.
The reformer heat exchanger 10 has a reformed gas channel 11 and a combustion gas channel 12, and the reformed gas channel 11 is reformed on the inner surface including the heat transfer fins for reforming reaction. A catalyst (noble metal, nickel, etc.) is supported. The reforming catalyst may be one in which pellets are arranged in the flow path instead of being supported on the flow path wall surface.
A reformed gas (including reformed raw material) flows through the reformed gas passage 11, and a combustion gas flows through the combustion gas passage 12. The reformed gas and the combustion gas do not mix with each other. The flow of the reformed gas that flows through the reformed gas passage 11 and the flow of the combustion gas that flows through the combustion gas passage 12 are opposite to each other.

改質器用熱交換器１０は、複数の熱交換部１３を有する。改質ガスは複数の熱交換部１３を直列に流れ、燃焼ガスは複数の熱交換部１３を並列に流れる。
図１、図２は、熱交換部１３が２段（第１段の熱交換部１３Ａ、第２段の熱交換部１３Ｂ）設けられた場合を示すが、熱交換部１３の数は２とは限らず、３以上であってもよい。複数の熱交換部１３Ａ、１３Ｂは、単一の積層型熱交換器を複数段に分離壁１６で仕切って形成されてもよいし、あるいは、別々の熱交換器から形成されてもよい。 The reformer heat exchanger 10 includes a plurality of heat exchange units 13. The reformed gas flows through the plurality of heat exchange units 13 in series, and the combustion gas flows through the plurality of heat exchange units 13 in parallel.
1 and 2 show a case where the heat exchange section 13 is provided in two stages (a first stage heat exchange section 13A and a second stage heat exchange section 13B). The number of heat exchange sections 13 is two. The number is not limited, and may be 3 or more. The plurality of heat exchange units 13A and 13B may be formed by dividing a single stacked heat exchanger into a plurality of stages by the separation wall 16, or may be formed by separate heat exchangers.

図１は図３のＤ−Ｄ断面を示しており、燃焼ガス流路１２を示している。改質ガス流路１１は図３のＣ−Ｃ断面にあり、Ｄ−Ｄ断面とは異なる断面であり、図１の紙面とは異なる面にある。図２は、図１のＫ−Ｋ線に沿った断面を示す。 FIG. 1 shows a DD cross section of FIG. 3 and shows a combustion gas passage 12. The reformed gas flow path 11 is in the CC cross section of FIG. 3, is a cross section different from the DD cross section, and is in a plane different from the paper surface of FIG. FIG. 2 shows a cross section taken along line KK of FIG.

図１の紙面と異なる面内において、改質ガスは、まず第１段の熱交換部１３Ａに流入し、ついで第１段の熱交換部１３Ａから流出し、ついで、第２段の熱交換部１３Ｂに流入し、ついで第２段の熱交換部１３Ｂから流出する。 In a plane different from that of FIG. 1, the reformed gas first flows into the first stage heat exchange section 13A, then flows out from the first stage heat exchange section 13A, and then the second stage heat exchange section. It flows into 13B, and then flows out from the second stage heat exchange section 13B.

図１の紙面内において、燃焼ガスは、燃焼ガス入口マニホールド１４Ａから第１段の熱交換部１３Ａに流入し、第１段の熱交換部１３Ａを改質ガスと対向して流れ、ついで第１段の熱交換部１３Ａから燃焼ガス出口マニホールド１５Ａに流出する。
燃焼ガスは、第１段の熱交換部１３Ａを流れるのとは別に、燃焼ガス入口マニホールド１４Ｂから第２段の熱交換部１３Ｂに流入し、第２段の熱交換部１３Ｂを改質ガスと対向して流れ、ついで第２段の熱交換部１３Ｂから燃焼ガス出口マニホールド１５Ｂに流出する。
第１段の熱交換部１３Ａの燃焼ガスの流れと第２段の熱交換部１３Ｂの燃焼ガスの流れとは、互いに並列である。第１段の熱交換部１３Ａの燃焼ガスの流れと第２段の熱交換部１３Ｂの燃焼ガスの流れとは、分離壁１６によって、互いに隔てられる。 In FIG. 1, the combustion gas flows from the combustion gas inlet manifold 14A into the first stage heat exchange section 13A, flows through the first stage heat exchange section 13A facing the reformed gas, and then the first stage. Outflow from the stage heat exchange section 13A to the combustion gas outlet manifold 15A.
The combustion gas flows from the combustion gas inlet manifold 14B into the second stage heat exchange section 13B separately from flowing through the first stage heat exchange section 13A, and the second stage heat exchange section 13B serves as the reformed gas. It flows oppositely, and then flows out from the second stage heat exchange section 13B to the combustion gas outlet manifold 15B.
The flow of the combustion gas in the first stage heat exchange unit 13A and the flow of the combustion gas in the second stage heat exchange unit 13B are parallel to each other. The flow of the combustion gas in the first stage heat exchange section 13A and the flow of the combustion gas in the second stage heat exchange section 13B are separated from each other by the separation wall 16.

１７は燃焼ガスと改質ガスとを分離しシールするシール部であり、１８は改質部外壁１９と熱交換部１３との間をシールして改質ガスが熱交換部１３を通過せずに吹き抜けることを防止するシール部である。
各熱交換部１３は、伝熱フィンを有する。２０は改質ガス側伝熱フィンを示し、２１は燃焼ガス側伝熱フィンを示す。 Reference numeral 17 denotes a seal part that separates and seals the combustion gas and the reformed gas. Reference numeral 18 denotes a seal between the reformer outer wall 19 and the heat exchange part 13 so that the reformed gas does not pass through the heat exchange part 13. It is a seal part which prevents blowing through.
Each heat exchange unit 13 has heat transfer fins. Reference numeral 20 denotes a reformed gas side heat transfer fin, and reference numeral 21 denotes a combustion gas side heat transfer fin.

図３に示すように、改質器用熱交換器１０は、改質ガス側伝熱フィン２０、積層プレート２２、燃焼ガス側伝熱フィン２１、積層プレート２２を順に積層した、積層型熱交換器から構成されてもよい。
改質ガス側伝熱フィン２０の表面および積層プレート２２の改質ガス側表面には、改質触媒が担持される。
積層プレート２２の中央に分離壁１６が設けられていて、熱交換部１３を複数の熱交換部１３Ａ、１３Ｂに分離している。 As shown in FIG. 3, the reformer heat exchanger 10 is a stacked heat exchanger in which a reformed gas side heat transfer fin 20, a stacked plate 22, a combustion gas side heat transfer fin 21, and a stacked plate 22 are stacked in this order. May be configured.
A reforming catalyst is supported on the surface of the reformed gas side heat transfer fin 20 and the reformed gas side surface of the laminated plate 22.
A separation wall 16 is provided at the center of the laminated plate 22 and separates the heat exchange unit 13 into a plurality of heat exchange units 13A and 13B.

つぎに、本発明の改質器用熱交換器１０の作用、効果を説明する。 Next, functions and effects of the heat exchanger 10 for reformer of the present invention will be described.

改質ガス流路１１に対して、高温熱媒体（燃焼ガス）との熱交換部１３が、複数箇所（第１の熱交換部１３Ａ、第２の熱交換部１３Ｂ）、互いに直列に形成され、各熱交換部に燃焼ガスが並列に供給されるので、各熱交換部１３Ａ、１３Ｂで改質ガスと燃焼ガスとの熱交換が行われ、改質ガス入口部Ｆ近傍（改質ガス温度が触媒活性化温度に上がって、一定温度領域に入った直後の領域）での改質ガスと燃焼ガスとの温度差が大きくなり、改質ガス入口部Ｆ近傍での燃焼ガスから改質ガスへの伝達熱量が増える。その結果、改質ガス入口部Ｆ近傍での改質ガスへの熱の供給不足が解消され、改質ガス入口部近傍の熱伝達律速が解消され、吸熱改質反応が促進される。 With respect to the reformed gas flow path 11, heat exchange portions 13 with a high-temperature heat medium (combustion gas) are formed in a plurality of locations (first heat exchange portion 13 A and second heat exchange portion 13 B) in series with each other. Since the combustion gas is supplied to each heat exchange unit in parallel, the heat exchange between the reformed gas and the combustion gas is performed in each heat exchange unit 13A, 13B, and the vicinity of the reformed gas inlet F (reformed gas temperature). The temperature difference between the reformed gas and the combustion gas in the region immediately after the catalyst reaches the catalyst activation temperature and enters the constant temperature region) increases, and the reformed gas is changed from the combustion gas in the vicinity of the reformed gas inlet F. The amount of heat transferred to the As a result, the shortage of heat supply to the reformed gas in the vicinity of the reformed gas inlet F is eliminated, the heat transfer rate limiting in the vicinity of the reformed gas inlet is eliminated, and the endothermic reforming reaction is promoted.

また、複数の熱交換部１３の各熱交換部１３Ａ、１３Ｂにおいて吸熱改質反応が促進されることにより、吸熱改質反応が行われている一定温度領域が拡大し（改質ガス出口部Ｅ側に拡大し）、その結果、燃焼ガスの熱量の改質反応の吸熱への利用量が増え、広い領域において改質反応が促進される。また、改質ガスの出口部Ｅ近傍での改質ガスの温度上昇に使われる熱量が低減し、改質ガスの出口部Ｅ近傍の改質ガス温度が従来に比べて低減する。その結果、熱交換器の改質ガス流路の耐久性も向上する。 In addition, the endothermic reforming reaction is promoted in each of the heat exchanging sections 13A and 13B of the plurality of heat exchanging sections 13, thereby expanding a certain temperature region in which the endothermic reforming reaction is performed (reformed gas outlet section E As a result, the amount of heat of the combustion gas used for the heat absorption of the reforming reaction increases, and the reforming reaction is promoted in a wide region. In addition, the amount of heat used to raise the temperature of the reformed gas in the vicinity of the reformed gas outlet E is reduced, and the reformed gas temperature in the vicinity of the reformed gas outlet E is reduced as compared with the prior art. As a result, the durability of the reformed gas flow path of the heat exchanger is also improved.

また、熱交換部１３が積層型熱交換器であるため、熱交換部１３Ａ、１３Ｂが別体の場合に比べて、熱交換器がコンパクトになる。その結果、コストダウン、車両への搭載性に有利等の種々の利点がある。 In addition, since the heat exchange unit 13 is a stacked heat exchanger, the heat exchanger is more compact than when the heat exchange units 13A and 13B are separate. As a result, there are various advantages such as cost reduction and advantageous mounting on a vehicle.

本発明の改質器用熱交換器の燃焼ガス流路部分の断面図である。It is sectional drawing of the combustion gas flow-path part of the heat exchanger for reformers of this invention. 図１の改質器用熱交換器のＫ−Ｋ線断面図である。It is the KK sectional view taken on the line of the heat exchanger for reformers of FIG. 図２の改質器用熱交換器の積層コア部品の斜視図である。It is a perspective view of the lamination | stacking core component of the heat exchanger for reformers of FIG. 本発明の改質器用熱交換器の、燃焼ガス、改質ガスの温度と燃焼ガス、改質ガスの流れ方向位置との関係を示すグラフである。It is a graph which shows the relationship between the temperature of combustion gas and reformed gas, and the flow direction position of combustion gas and reformed gas of the heat exchanger for reformers of this invention. 本出願人が従来開発してきた改質器用熱交換器の改質ガス流路部分の断面図（図７のＣ−Ｃ断面図）である。It is sectional drawing (CC sectional drawing of FIG. 7) of the reformed gas flow path part of the heat exchanger for reformers conventionally developed by this applicant. 図５の改質器用熱交換器の燃焼ガス流路部分の断面図（図７のＣ−Ｃ断面図）である。It is sectional drawing (CC sectional drawing of FIG. 7) of the combustion gas flow-path part of the heat exchanger for reformers of FIG. 図５の改質器用熱交換器の積層コア部品の斜視図である。It is a perspective view of the lamination | stacking core component of the heat exchanger for reformers of FIG. 図５の改質器用熱交換器の、燃焼ガス、改質ガスの温度と燃焼ガス、改質ガスの流れ方向位置との関係を示すグラフである。It is a graph which shows the relationship between the temperature of combustion gas and reformed gas, and the flow direction position of combustion gas and reformed gas of the heat exchanger for reformers of FIG.

Explanation of symbols

１０改質器用熱交換器
１１改質ガス流路
１２燃焼ガス流路
１３熱交換部
１３Ａ第１の熱交換部
１３Ｂ第２の熱交換部
１４Ａ（第１の熱交換部Ａに対する）燃焼ガス入口マニホールド
１４Ｂ（第２の熱交換部Ｂに対する）燃焼ガス入口マニホールド
１５Ａ（第１の熱交換部Ａに対する）燃焼ガス出口マニホールド
１５Ｂ（第２の熱交換部Ｂに対する）燃焼ガス出口マニホールド
１６分離壁
１７シール部
１８シール部
１９改質部外壁
２０改質ガス伝熱フィン
２１燃焼ガス伝熱フィン DESCRIPTION OF SYMBOLS 10 Reformer heat exchanger 11 Reformed gas flow path 12 Combustion gas flow path 13 Heat exchange part 13A 1st heat exchange part 13B 2nd heat exchange part 14A (with respect to 1st heat exchange part A) Combustion gas inlet Manifold 14B Combustion gas inlet manifold 15A (for the second heat exchange section B) Combustion gas outlet manifold 15B (for the first heat exchange section A) Combustion gas outlet manifold 16 (for the second heat exchange section B) Separation wall 17 Seal portion 18 Seal portion 19 Reformer outer wall 20 Reformed gas heat transfer fin 21 Combustion gas heat transfer fin

Claims

A heat exchanger for a reformer with an endothermic reaction, wherein a plurality of heat exchange portions with a high-temperature heat medium are formed in the reformed gas flow path, and the high-temperature heat medium is provided for each heat exchange portion. Heat exchanger for reformer supplied in parallel.

The heat exchanger for a reformer according to claim 1, wherein the heat exchange unit is a stacked heat exchanger.