JPH0685867B2 - Heat exchanger type reformer - Google Patents
Heat exchanger type reformerInfo
- Publication number
- JPH0685867B2 JPH0685867B2 JP3046891A JP4689191A JPH0685867B2 JP H0685867 B2 JPH0685867 B2 JP H0685867B2 JP 3046891 A JP3046891 A JP 3046891A JP 4689191 A JP4689191 A JP 4689191A JP H0685867 B2 JPH0685867 B2 JP H0685867B2
- Authority
- JP
- Japan
- Prior art keywords
- tube
- heat transfer
- catalyst
- heat exchanger
- net
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000003054 catalyst Substances 0.000 claims description 51
- 230000001737 promoting effect Effects 0.000 claims description 22
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 239000007789 gas Substances 0.000 claims description 17
- 239000003345 natural gas Substances 0.000 claims description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 239000000567 combustion gas Substances 0.000 description 17
- 230000000694 effects Effects 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 230000004907 flux Effects 0.000 description 5
- 238000010248 power generation Methods 0.000 description 5
- 238000002407 reforming Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000011810 insulating material Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、溶融炭酸塩型燃料電池
（ＭＣＦＣ）発電システムにおいて、燃料電池アノード
排ガスを燃焼して得られる高温ガスの顕熱を利用して、
天然ガスをスチームで改質することにより水素および一
酸化炭素に富むガスを製造し、燃料電池アノードに供給
する役割をもつ改質触媒管を有する熱交換器型改質器に
関し、さらに詳しくは、その触媒管における伝熱効率が
高められた熱交換器型改質器に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention utilizes the sensible heat of high temperature gas obtained by burning the exhaust gas of a fuel cell anode in a molten carbonate fuel cell (MCFC) power generation system.
A heat exchanger type reformer having a reforming catalyst tube having a role of producing a gas rich in hydrogen and carbon monoxide by reforming natural gas with steam and supplying the gas to a fuel cell anode, and more specifically, The present invention relates to a heat exchanger type reformer having improved heat transfer efficiency in its catalyst tube.
【０００２】[0002]
【従来の技術】ＭＣＦＣ発電システムにおける改質器に
おいては、デイリースタート／シャット（ＤＳＳ）を含
む頻繁な起動・停止および急激な負荷変動にも耐え得る
熱衝撃に強い構造が要求され、このため、２重管構造を
もついわゆるバヨネットタイプの触媒管が多く採用され
る。図１はその構造の概略を示す断面図で、バヨネット
タイプ触媒管１は外管２と内管３との間に触媒層４が設
けられた構造のものである。天然ガスおよびスチームは
触媒層４をＡ方向に通過する間に水素と一酸化炭素に富
む改質ガスに改質される。この天然ガスの改質反応は、
たとえば反応式 ＣＨ4 ＋Ｈ2 Ｏ→ＣＯ＋３Ｈ2 ΔＨ＝４９．３Ｋｃａｌ／グラムモル で示される吸熱反応である。したがって、この改質反応
を促進するためにアノード排ガス燃焼器から排出される
高温の燃焼ガス流Ｂおよび内管を触媒層とは逆方向に流
れる改質ガスからの熱を触媒層４に伝熱して触媒層４を
適度な温度に保持するようにしている。2. Description of the Related Art A reformer in an MCFC power generation system is required to have a structure resistant to thermal shock, which can withstand frequent start / stop including daily start / shut (DSS) and abrupt load change. A so-called bayonet type catalyst tube having a double tube structure is often used. FIG. 1 is a cross-sectional view showing the outline of the structure, and a bayonet type catalyst tube 1 has a structure in which a catalyst layer 4 is provided between an outer tube 2 and an inner tube 3. Natural gas and steam are reformed into a reformed gas rich in hydrogen and carbon monoxide while passing through the catalyst layer 4 in the A direction. This natural gas reforming reaction is
For example, it is an endothermic reaction represented by the reaction formula CH 4 + H 2 O → CO + 3H 2 ΔH = 49.3 Kcal / gram mol. Therefore, in order to promote this reforming reaction, the high temperature combustion gas flow B discharged from the anode exhaust gas combustor and the heat from the reformed gas flowing in the inner tube in the direction opposite to the catalyst layer are transferred to the catalyst layer 4. The catalyst layer 4 is kept at an appropriate temperature.
【０００３】このようなバヨネットタイプの触媒管に対
して外側（シェル側）を流通する高温燃焼ガスから必要
な熱量を供給する系においては、特に次の点が伝熱特性
上重要である。 (1) 伝熱効率を高めること。 (2) ヒートフラックスの平均値を高めること。 (3) 複数の触媒管を均等加熱すること。そのために圧
力損失ΔＰを所望の値（０．０５〜０．１kg/cm 2 ）に
維持するとともにその分布を制御して燃焼ガスの偏流を
避けること。In a system for supplying a necessary amount of heat from a high temperature combustion gas flowing on the outside (shell side) to such a bayonet type catalyst tube, the following points are particularly important in terms of heat transfer characteristics. (1) To improve heat transfer efficiency. (2) To increase the average value of heat flux. (3) To uniformly heat multiple catalyst tubes. Therefore, maintain the pressure loss ΔP at a desired value (0.05 to 0.1 kg / cm 2 ) and control its distribution to avoid drift of the combustion gas.
【０００４】したがって、触媒層への伝熱効率を高める
ために、従来種々の工夫がなされている。図２は従来技
術における伝熱促進手段を示す要部断面図であり、たと
えば、図２（ａ）に示すように触媒管内管内側にスリー
ブ５を設けたもの、燃焼ガス側に図２（ｂ）に示すよう
にスリーブ６を設けたもの、図２（ｃ）に示すようにオ
リフィスバッフル７を設けたもの、図２（ｄ）に示すよ
うに外管外側にワイヤーネット８を設けたもの、図２
（ｅ）に示すように充填物９を施したものなどがある。Therefore, in order to improve the heat transfer efficiency to the catalyst layer, various measures have been conventionally made. FIG. 2 is a cross-sectional view of an essential part showing a heat transfer promoting means in the prior art. For example, as shown in FIG. 2 (a), a sleeve 5 is provided inside the inner tube of the catalyst tube, and FIG. ), A sleeve 6 is provided as shown in FIG. 2C, an orifice baffle 7 is provided as shown in FIG. 2C, and a wire net 8 is provided outside the outer tube as shown in FIG. 2D. Figure 2
As shown in (e), there is a case where the filling material 9 is applied.
【０００５】しかし、触媒管内管内側にスリーブを設け
たもの（図２（ａ））では、伝熱促進効果が低いために
ほぼ内管全領域に設置する必要があり、したがって、内
管側ヒートフラックス（熱流束）分布の制御が困難とな
り、また、触媒管が３重構造となり複雑化する。燃焼ガ
ス側にスリーブまたはオリフィスバッフルを設けたもの
（図２（ｂ）または（ｃ））は、それら単独では伝熱促
進効果が低いため広範囲に設置する必要があり、ヒート
フラックス分布の制御が困難である。燃焼ガス側にワイ
ヤーネットを設けたもの（図２（ｄ））では、伝熱促進
効果は高いが、それ単独では燃焼ガス側の圧力損失が小
さすぎてその分布の制御が困難であるため、燃焼ガスの
偏流の防止が難しく、したがって複数の触媒管の均等加
熱が困難となる。燃焼ガス側にスリーブおよびワイヤー
ネットを設けたもの（図２（ｂ）と（ｄ）の組合せ）で
は、伝熱促進効果に関しては良好であるが、燃焼ガス側
の圧力損失を最適水準（たとえば、０．０５〜０．１kg
/cm 2 ）に保つためには設置領域を拡大する必要があ
る。また、伝熱促進効果を高めるためにスリーブと外管
とのクリアランスを小さくしようとすると、製作、取付
け上の精度が問題となる。燃焼ガス側に充填物を施した
もの（図２（ｅ））では、伝熱促進効果を高めることは
できるが、燃焼ガス側の圧力損失が過大となり、かつそ
の分布の制御もできない。However, in the case where a sleeve is provided inside the inner tube of the catalyst tube (FIG. 2 (a)), the effect of promoting heat transfer is low, and therefore it is necessary to install it in almost the entire area of the inner tube. It becomes difficult to control the flux (heat flux) distribution, and the catalyst tube has a triple structure and becomes complicated. The one provided with a sleeve or an orifice baffle on the combustion gas side (FIG. 2 (b) or (c)) needs to be installed in a wide range because it has a low heat transfer promotion effect by itself, and it is difficult to control the heat flux distribution. Is. In the case where the wire net is provided on the combustion gas side (Fig. 2 (d)), the heat transfer promotion effect is high, but by itself it is difficult to control the distribution because the pressure loss on the combustion gas side is too small. It is difficult to prevent uneven flow of the combustion gas, and thus it is difficult to uniformly heat the plurality of catalyst tubes. In the case where the sleeve and the wire net are provided on the combustion gas side (combination of FIGS. 2B and 2D), the heat transfer promotion effect is good, but the pressure loss on the combustion gas side is at the optimum level (for example, 0.05-0.1kg
/ cm 2 ), it is necessary to enlarge the installation area. Further, if the clearance between the sleeve and the outer tube is reduced in order to enhance the effect of promoting heat transfer, the accuracy in manufacturing and mounting becomes a problem. In the case where the combustion gas side is filled (FIG. 2 (e)), the heat transfer promotion effect can be enhanced, but the pressure loss on the combustion gas side becomes excessive and the distribution thereof cannot be controlled.
【０００６】[0006]
【発明が解決しようとする課題】本発明は、このような
従来技術の欠点を解決し、さらに伝熱効率を高めるとと
もに触媒管の均等加熱を可能にしかつ装置のコンパクト
化を実現する熱交換器型改質器を提供することを目的と
する。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned drawbacks of the prior art, further enhances the heat transfer efficiency, enables uniform heating of the catalyst tubes, and realizes a compact apparatus. An object is to provide a reformer.
【０００７】[0007]
【課題を解決するための手段】上記課題を解決するため
には、触媒管内管側にデミスターネットおよびワイヤー
ネットからなる伝熱促進手段を設ければ伝熱効率が著し
く改善され極めて有効であることに着目して、本発明は
完成された。In order to solve the above-mentioned problems, it is extremely effective that the heat transfer efficiency is remarkably improved by providing a heat transfer promoting means composed of a demister net and a wire net on the inner tube side of the catalyst tube. Focusing attention, the present invention has been completed.
【０００８】すなわち、本発明の熱交換器型改質器は、
天然ガスとスチームとを反応させて水素および一酸化炭
素に富むガスに改質するための内管と外管からなる２重
管構造のバヨネットタイプ触媒管を具備する熱交換器型
改質器において、前記触媒管の内管内側にデミスターネ
ットおよび内管ワイヤーネットの組合せからなる伝熱促
進手段を設けてなること、を特徴とするものである。That is, the heat exchanger type reformer of the present invention is
In a heat exchanger type reformer equipped with a bayonet type catalyst tube having a double tube structure composed of an inner tube and an outer tube for reacting natural gas with steam to reform it into a gas rich in hydrogen and carbon monoxide The heat transfer promoting means, which is a combination of a demister net and an inner tube wire net, is provided inside the inner tube of the catalyst tube.
【０００９】本発明の好ましい態様において、前記触媒
管の外側に外管ワイヤーネットおよびオリフィスバッフ
ルからなる伝熱促進手段をさらに設けてなるものとする
ことができる。In a preferred aspect of the present invention, heat transfer promoting means composed of an outer tube wire net and an orifice baffle may be further provided outside the catalyst tube.
【００１０】発明の具体的説明 以下、図面を含めて本発明の内容を具体的に説明する。
本発明の熱交換器型改質器において、天然ガスをスチー
ムで改質するために用いる触媒管としては、従来用いら
れているバヨネットタイプ触媒管が使用され、その構造
の概要は図１に示したものと同様である。 Detailed Description of the Invention Hereinafter, the content of the present invention will be specifically described with reference to the drawings.
In the heat exchanger type reformer of the present invention, a conventionally used bayonet type catalyst tube is used as a catalyst tube used for reforming natural gas with steam, and an outline of the structure is shown in FIG. It is similar to
【００１１】図３は、本発明における好ましい態様の伝
熱促進手段を説明する要部断面図である。バヨネットタ
イプ触媒管１の内管３の内側にはデミスターネット１０
および内管ワイヤーネット１１を組合わせてなる伝熱促
進手段が設けられる。このデミスターネットは、細い金
属性のワイヤーをランダムに、たとえば金タワシの如く
集積体の形態に形成してなるもので、たとえば空隙率９
９％、密度８０ｋｇ／ｍ3 程度のものが用いられる。ま
た、内管ワイヤーネットは、上記のデミスターネットを
圧縮したような形態のもので、たとえばその空隙が２０
メッシュ程度のものである。この内管ワイヤーネットは
それ自身伝熱促進効果を持つとともにデミスターネット
を保持し、また改質ガス流の整流作用をする。FIG. 3 is a cross-sectional view of essential parts for explaining a heat transfer promoting means of a preferred embodiment of the present invention. A demister net 10 is provided inside the inner tube 3 of the bayonet type catalyst tube 1.
Further, a heat transfer promoting means formed by combining the inner tube wire net 11 is provided. This demister net is formed by randomly forming thin metal wires in the form of an integrated body such as a gold scourer, and has a porosity of 9
9% and a density of about 80 kg / m 3 are used. Further, the inner pipe wire net is in a form in which the above-mentioned demister net is compressed, and for example, the void has 20
It is about a mesh. This inner tube wire net has an effect of promoting heat transfer by itself, holds the demister net, and also has a function of rectifying the reformed gas flow.
【００１２】このような金属ワイヤーの集積体が、伝熱
促進作用をするのは次の理由による。すなわち、このよ
うな金属ワイヤーの集積体の場合、比表面積が大きく、
高温の改質ガス流体の通路内に配置されることにより、
改質ガス流体により容易に高温に加熱される。この高温
の金属ワイヤー集積体の輻射能は大きいため、被加熱面
すなわち触媒層内管表面は、改質ガス流体による対流加
熱に加えて、この金属ワイヤー集積体からの熱輻射によ
る輻射加熱を受け、しかもその熱輻射による熱伝達量は
大きい。その結果、改質ガス流体からの被加熱表面への
全体的な熱伝達は、金属ワイヤー集積体を用いない場合
の熱伝達に比べて著しく大きくなる。The reason why such an aggregate of metal wires has a function of promoting heat transfer is as follows. That is, in the case of such an aggregate of metal wires, the specific surface area is large,
By being placed in the passage of the hot reformed gas fluid,
It is easily heated to high temperature by the reformed gas fluid. Since the radiant power of this high-temperature metal wire assembly is high, the surface to be heated, that is, the inner surface of the catalyst layer tube, is subjected to radiant heating due to thermal radiation from the metal wire assembly in addition to convection heating by the reforming gas fluid. Moreover, the amount of heat transfer by the heat radiation is large. As a result, the overall heat transfer from the reformed gas fluid to the heated surface is significantly greater than that without the metal wire assembly.
【００１３】このデミスターネットおよび内管ワイヤー
ネットは、これらを触媒管内管の縦方向に交互に設けて
多段に組合せるのがデミスターネットを保持する上で好
ましい。またデミスターネットの厚み（ｌｎ）と内管ワ
イヤーネットの厚み（ｌｗ）の比率（ｌｎ／ｌｗ）は、
３〜２０、好ましくは８〜１２の範囲とする。このデミ
スターネット１０および内管ワイヤーネット１１を組合
せてなる伝熱促進手段は、触媒管内管の内側に設置され
るが、必ずしも触媒層出口（図１の１２で示す）から触
媒管内管出口（図１の１３で示す）までの全領域に亘っ
て設置する必要はなく、好ましくは内管長の３０〜８０
％の領域に亘って設置する。The demister net and the inner tube wire net are preferably provided alternately in the longitudinal direction of the inner tube of the catalyst tube and combined in multiple stages in order to retain the demister net. The ratio (ln / lw) of the thickness (ln) of the demister net and the thickness (lw) of the inner tube wire net is
The range is 3 to 20, preferably 8 to 12. The heat transfer promoting means formed by combining the demister net 10 and the inner tube wire net 11 is installed inside the inner tube of the catalyst tube, but is not necessarily from the catalyst layer outlet (indicated by 12 in FIG. 1) to the catalyst tube inner tube outlet (see FIG. 1). It is not necessary to install over the entire area up to 13) of 1), preferably 30 to 80 of the inner pipe length.
% Over the area.
【００１４】なお、本ＭＣＦＣ発電システム用改質器の
運転温度は改質ガスの触媒層出口で８００℃程度、触媒
管内管出口で６００℃程度であるが、この温度範囲で
は、ＣＯリッチガスからのブドアール反応、すなわち、
２ＣＯ→Ｃ＋ＣＯ2 による炭素析出の可能性が大で
ある。これを防ぐために触媒管の内管だけでなく上記の
内管内側の伝熱促進手段に用いる材料として、ブドアー
ル反応を抑制もしくは少なくとも触媒作用を有しない材
質のものが選択される。また、運転条件においても、ス
チーム／カーボン比（Ｓ／Ｃ）として天然ガス原料とし
ては一般に採用される２〜２．５よりも稍大の３程度を
採用する等して、ブドアール反応を抑制することが好ま
しい。The operating temperature of the reformer for the present MCFC power generation system is about 800 ° C. at the outlet of the reformed gas catalyst layer and about 600 ° C. at the outlet of the inside of the catalyst pipe. The Boudard reaction, ie
There is a high possibility of carbon precipitation due to 2CO → C + CO 2 . In order to prevent this, as a material used not only for the inner tube of the catalyst tube but also for the heat transfer promoting means inside the inner tube, a material which suppresses the Boudard reaction or at least has no catalytic action is selected. In addition, even under operating conditions, the steam / carbon ratio (S / C) of about 3 which is larger than 2 to 2.5 that is generally adopted as a natural gas raw material is adopted to suppress the Buddard reaction. It is preferable.
【００１５】本発明の好ましい態様においては、上記の
デミスターネットおよび内管ワイヤーネットを組合せて
なる伝熱促進手段に加えて、さらに図３に示すように触
媒管外側に外管ワイヤーネット１４およびオリフィスバ
ッフル１５からなる伝熱促進手段が設けられる。なお、
オリフィスバッフル１５は複数段設けられるが、これら
はタイロッド１６によって支持される。このような更な
る伝熱促進手段を設けることによって熱伝達がさらに改
良される。In a preferred embodiment of the present invention, in addition to the heat transfer promoting means formed by combining the demister net and the inner tube wire net described above, an outer tube wire net 14 and an orifice are provided outside the catalyst tube as shown in FIG. A heat transfer promoting means including the baffle 15 is provided. In addition,
The orifice baffle 15 is provided in a plurality of stages, but these are supported by a tie rod 16. Heat transfer is further improved by providing such additional heat transfer enhancing means.
【００１６】ここで、外管ワイヤーネット１４は上述の
デミスターネットおよび内管ワイヤーネットを組合せて
なる伝熱促進手段とほぼ同様に対流加熱と輻射加熱とに
よる熱伝達作用をなし、たとえば１．１φ、８メッシュ
程度のものが好ましく用いられる。また、オリフィスバ
ッフル１５を設置することにより、高温の燃焼ガス流路
がその設置位置において狭くなり、燃焼ガスの流れに乱
れを生じて伝熱促進作用をするとともに燃焼ガスが偏流
なく流通することを可能にする最適圧力損失０．０５〜
０．１kg/cm 2 を与える。The outer tube wire net 14 has a heat transfer function by convection heating and radiant heating, which is similar to the heat transfer promoting means formed by combining the above-mentioned demister net and inner tube wire net, and is 1.1φ, for example. , About 8 mesh is preferably used. Further, by installing the orifice baffle 15, the high temperature combustion gas flow path becomes narrow at its installation position, which disturbs the flow of the combustion gas to promote heat transfer and also allows the combustion gas to flow without uneven flow. Optimum pressure loss that enables 0.05 ~
Give 0.1 kg / cm 2 .
【００１７】この外管ワイヤーネット１４およびオリフ
ィスバッフル１５からなる伝熱促進手段は、触媒管外側
に設置されるが、その全領域に亘って設ける必要はな
い。図４は、本発明のＭＣＦＣ発電用熱交換器型改質器
の構造の概要を説明する断面図である。本改質器本体の
上部には、天然ガスおよびスチームの入口ノズル１７、
改質ガスの出口ノズル１８を有し、改質器本体内部には
触媒管１が複数本たとえば６本（図では２本のみ示し
た）設置され、その触媒管の上部外側にはオリフィスバ
ッフル１５がタイロッド１６で支持されて複数段（図で
は５段）および外管ワイヤーネット（図示せず）が設け
られている。また触媒管１の内管３の内側にはデミスタ
ーネットおよび内管ワイヤーネットの組合せからなる伝
熱促進手段（図示せず）が設けられる。改質器本体下部
には燃焼ガスの入口ノズル１９が、上部にはその出口ノ
ズル２０が設けられている。これらの伝熱促進手段の設
置によって、触媒層への伝熱効率が高められ、またヒー
トフラックスの平均値が高められるとともに燃焼ガス流
の偏流なく複数の触媒管の均等加熱が実現される。The heat transfer promoting means consisting of the outer tube wire net 14 and the orifice baffle 15 is installed outside the catalyst tube, but it is not necessary to provide it over the entire area thereof. FIG. 4 is a cross-sectional view illustrating the outline of the structure of the heat exchanger type reformer for MCFC power generation of the present invention. In the upper part of the main body of the reformer, an inlet nozzle 17 for natural gas and steam,
A reforming gas outlet nozzle 18 is provided, and a plurality of, for example, six catalyst tubes 1 (only two are shown in the figure) are installed inside the reformer main body, and an orifice baffle 15 is provided outside the upper part of the catalyst tubes. Are supported by tie rods 16 and are provided with a plurality of stages (5 stages in the figure) and an outer tube wire net (not shown). Further, inside the inner tube 3 of the catalyst tube 1, heat transfer promoting means (not shown) composed of a combination of a demister net and an inner tube wire net is provided. A combustion gas inlet nozzle 19 is provided in the lower portion of the reformer main body, and an outlet nozzle 20 thereof is provided in the upper portion. By installing these heat transfer promoting means, the heat transfer efficiency to the catalyst layer is increased, the average value of the heat flux is increased, and uniform heating of the plurality of catalyst tubes is realized without uneven distribution of the combustion gas flow.
【００１８】触媒管１の設置されている部分に対応する
内壁は、熱容量の小さなセラミックファイバーブランケ
ット２１で、本体下部の内壁は耐火物キャスタブル２２
でライニングされ、それらの外壁は断熱材キャスタブル
２３で構成されており、また、改質器本体の上部の外壁
は別の断熱材２４で形成されている。The inner wall corresponding to the installed portion of the catalyst tube 1 is a ceramic fiber blanket 21 having a small heat capacity, and the inner wall at the bottom of the main body is a refractory castable 22.
The outer wall of the reformer main body is formed of another heat insulating material 24, and the outer wall of the reformer main body is formed of another heat insulating material 24.
【００１９】そして、天然ガスおよびスチームは入口ノ
ズル１７から本改質器内に導入され、触媒管１の触媒層
を通過する間に水素と一酸化炭素に富むガスに改質され
出口ノズル１８から排出される。一方、高温の燃焼ガス
は入口ノズル１９から改質器本体内に導入され触媒管１
に熱を伝達した後出口ノズル２０から排出される。Then, natural gas and steam are introduced into the reformer from the inlet nozzle 17, are reformed into a gas rich in hydrogen and carbon monoxide while passing through the catalyst layer of the catalyst tube 1, and are discharged from the outlet nozzle 18. Is discharged. On the other hand, the high temperature combustion gas is introduced into the reformer main body through the inlet nozzle 19 and the catalyst tube 1
After transferring the heat to the outlet nozzle 20, it is discharged from the outlet nozzle 20.
【００２０】[0020]
【発明の効果】本発明によれば、触媒管の内管内側にデ
ミスターネットおよび内管ワイヤーネットを組合せてな
る伝熱促進手段を設置したので、著しい熱伝達の改善が
図られ、装置のコンパクト化が可能となるとともに複数
の触媒管の均等加熱を実現できる。According to the present invention, the heat transfer promoting means, which is a combination of the demister net and the inner pipe wire net, is installed inside the inner tube of the catalyst tube, so that the heat transfer is remarkably improved and the apparatus is compact. It becomes possible to realize uniform heating of a plurality of catalyst tubes.
【図１】バヨネットタイプ触媒管の構造の概要を示す断
面図。FIG. 1 is a sectional view showing an outline of the structure of a bayonet type catalyst tube.
【図２】従来技術における伝熱促進手段を示す要部断面
図。FIG. 2 is a cross-sectional view of essential parts showing a heat transfer promoting means in a conventional technique.
【図３】本発明の好ましい態様の伝熱促進手段を説明す
る要部断面図。FIG. 3 is a cross-sectional view of an essential part for explaining a heat transfer promotion means of a preferred embodiment of the present invention.
【図４】本発明のＭＣＦＣ発電用熱交換器型改質器の構
造の概要を説明する断面図。FIG. 4 is a cross-sectional view illustrating the outline of the structure of a heat exchanger type reformer for MCFC power generation of the present invention.
１ バヨネットタイプ触媒管 ２ 外管 ３ 内管 ４ 触媒層 １０ デミスターネット １１ 内管ワイヤーネット １４ 外管ワイヤーネット １５ オリフィスバッフル 1 Bayonet type catalyst tube 2 Outer tube 3 Inner tube 4 Catalyst layer 10 Demister net 11 Inner tube wire net 14 Outer tube wire net 15 Orifice baffle
Claims (2)
よび一酸化炭素に富むガスに改質するための内管と外管
からなる２重管構造のバヨネットタイプ触媒管を具備す
る熱交換器型改質器において、前記触媒管の内管内側に
デミスターネットおよび内管ワイヤーネットの組合せか
らなる伝熱促進手段を設けてなることを特徴とする、熱
交換器型改質器。1. A heat exchanger comprising a bayonet type catalyst tube having a double tube structure composed of an inner tube and an outer tube for reacting natural gas with steam to reform it into a gas rich in hydrogen and carbon monoxide. A heat exchanger type reformer, characterized in that a heat transfer promoting means comprising a combination of a demister net and an inner pipe wire net is provided inside the inner tube of the catalyst tube.
よびオリフィスバッフルからなる伝熱促進手段をさらに
設けてなる、請求項１に記載の熱交換器型改質器。2. The heat exchanger type reformer according to claim 1, further comprising a heat transfer promoting means composed of an outer tube wire net and an orifice baffle outside the catalyst tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3046891A JPH0685867B2 (en) | 1991-03-12 | 1991-03-12 | Heat exchanger type reformer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3046891A JPH0685867B2 (en) | 1991-03-12 | 1991-03-12 | Heat exchanger type reformer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04285001A JPH04285001A (en) | 1992-10-09 |
| JPH0685867B2 true JPH0685867B2 (en) | 1994-11-02 |
Family
ID=12759987
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3046891A Expired - Fee Related JPH0685867B2 (en) | 1991-03-12 | 1991-03-12 | Heat exchanger type reformer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0685867B2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19717067C2 (en) * | 1997-04-23 | 1999-09-09 | Dbb Fuel Cell Engines Gmbh | Reforming reactor plant, in particular for steam reforming of methanol |
| US10894244B1 (en) * | 2020-03-17 | 2021-01-19 | Bayotech, Inc. | Hydrogen generation systems |
| US11608266B2 (en) * | 2020-03-17 | 2023-03-21 | Bayotech, Inc. | Hydrogen generation systems |
-
1991
- 1991-03-12 JP JP3046891A patent/JPH0685867B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH04285001A (en) | 1992-10-09 |
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| LAPS | Cancellation because of no payment of annual fees |