JPH0453804B2 - - Google Patents
Info
- Publication number
- JPH0453804B2 JPH0453804B2 JP58190424A JP19042483A JPH0453804B2 JP H0453804 B2 JPH0453804 B2 JP H0453804B2 JP 58190424 A JP58190424 A JP 58190424A JP 19042483 A JP19042483 A JP 19042483A JP H0453804 B2 JPH0453804 B2 JP H0453804B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- air
- retort
- endothermic
- catalyst
- 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 - Lifetime
Links
- 239000007789 gas Substances 0.000 claims description 86
- 239000003054 catalyst Substances 0.000 claims description 29
- 229930195733 hydrocarbon Natural products 0.000 claims description 28
- 150000002430 hydrocarbons Chemical class 0.000 claims description 28
- 239000004215 Carbon black (E152) Substances 0.000 claims description 27
- 238000010438 heat treatment Methods 0.000 claims description 23
- 239000001273 butane Substances 0.000 claims description 17
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 17
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 6
- 238000011426 transformation method Methods 0.000 claims description 4
- 239000011810 insulating material Substances 0.000 claims description 2
- 230000000149 penetrating effect Effects 0.000 claims 1
- 238000000034 method Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000004071 soot Substances 0.000 description 6
- JKTORXLUQLQJCM-UHFFFAOYSA-N 4-phosphonobutylphosphonic acid Chemical compound OP(O)(=O)CCCCP(O)(O)=O JKTORXLUQLQJCM-UHFFFAOYSA-N 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- 230000000171 quenching effect Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005255 carburizing Methods 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000005496 tempering Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000001294 propane 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
-
- 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
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Description
イ 産業上の利用分野
本発明は、吸熱型ガス変成方法およびその装置
に関し、詳しくは、鋼部品の焼入れ・焼もどし、
あるいは、浸炭焼入等の熱処理時に使用する吸熱
型ガスを、触媒を用いて850〜1100℃の高温で変
成させる、吸熱型ガス変成方法およびその装置に
かかる。
ロ 従来技術
鋼部品の焼入れ・焼もどし、あるいは、浸炭焼
入等の熱処理時に用いる吸熱室ガスは、従来、い
わゆる、RXガス発生炉と呼ばれる、吸熱室ガス
変成装置によつて製造されている。
そして、このRXガス発生炉は、ニツケル触媒
を充填し、850〜1100℃の高温に保持したレトル
ト内へ、メタン（CH4）プロパン（C3H8）、ブタ
ン（C4H10）等の炭化水素ガスと、空気との混合
ガスを送給し、CO、H2、N2を主成分とし、微量
のCH4、H2O、Ｃを含む、吸熱室ガスを変成させ
るものである。
さて、炭化水素ガスとして、ブタンに例をとつ
て、その変成反応を観察すると、レトルト内で
は、
C4H10＋202＋7.52N2→4CO＋5H＋7.52Nなる
反応が進行し、この時、以下の平衡反応が維持さ
れている。
H2＋CO2CO＋H2O
CH4＋CO22CO＋2H2
CH4＋H2OCO＋3H2
従つて、各成分の間には、CO≒23％、H2≒29
％、CH4＝微量〜0.2％、CO2＝微量〜20％、残
部N2で、互いに平衡状態にある。
そして、ブタンと空気との混合比を変化させる
と、その混合比に応じて、CH4、CO2、H2O等の
平衡値は変化する。
ところで、この従来の吸熱型ガス変成法におい
ては、炭化水素ガスと空気の混合ガスが、触媒と
接触して変成反応が進行する前に、炭化水素ガス
が熱分解して、すすＣを生成すると、平衡状態が
くずれて平衡ガスが得られなくなり、CO、CO2
によるカーボンテンシヤルの制御が困難となる欠
点がある。
さらに、上述のようにして生成されたすす
（Ｃ）が触媒に付着して、触媒活性の低下をきた
すという欠点がある。
上述のような、従来技術の欠点を、具体的な従
来装置に基づいて説明すると、第１図において、
ブタン１の0.86／minと空気２の8.6／minか
らなる混合ガスを、930℃のレトルト６に送給す
ると、100c.c.の触媒７のもとで、15／minの吸
熱室ガス３が変成できるものである。
ここで、従来の変成方法では、レトルト６にお
ける炭化水素ガスの熱分解を防止するため、急速
加熱部６ａは、細径パイプ数本からなる多管構造
として、加熱炉からの熱を吸収しやすくし、ガス
の急速加熱を促進するようにしてある
すなわち、この急速加熱部６ａでは、下記のよ
うなブタンの熱分解反応；
C4H10→Ｃ↓＋2CH4＋H2
によるすす（Ｃ）の生成を抑制するため、空気、
ブタンの混合ガスを急速加熱する必要がある。
しかし、従来の吸熱ガス変成装置のレトルト６
では、上述のように細径パイプの多管構造とし
て、急速加熱を促進すべく考慮されているもの
の、すす（Ｃ）の生成を、完全には抑制すること
ができない欠点がある。
ハ 発明の目的
本発明は、鋼部品の熱処理用雰囲気等に用いる
吸熱型ガスを、予め高温に加熱された空気に、直
接、室温の炭化水素ガスを混合させて、炭化水素
ガスを伝熱効率よく加熱し、炭化水素ガスの加熱
速度を速めることによつて、炭化水素ガスの熱分
解を確実に抑制でき、しかも、触媒反応による平
衡状態の吸熱型ガスを、効率よく変成することが
できる、吸熱型ガス変成方法およびその装置を提
供することを目的としている。
ニ 発明の構成
このような目的は、本発明によれば、触媒を充
填し、高温に保持されたレトルト内にブタン等の
炭化水素ガスと空気との混合ガスを供給して、吸
熱型ガスを変成させる、吸熱型ガス変成方法およ
びその装置であつて、
上記レトルトを、予熱室と触媒充填室にメツシ
ユ状隔膜により区画して、空気は、予熱室にて予
熱された後、触媒充填室に送給され、一方、ブタ
ン等の炭化水素ガスは、炭化水素ガスの熱分解を
防止するとともに、変成反応により平衡ガスを効
率的に得られるように、炉外配管により、予熱す
ることなく、直接、触媒充填室に送給することに
より、予熱された空気によつて、炭化水素ガスを
急速に加熱・混合し、嘱望と接触させて吸熱型ガ
スを変成することを特徴とした吸熱型ガス変成方
法、および、上記レトルトは、加熱炉内に配設さ
れるとともに、該レトルト内を空気予熱室と触媒
を充填した触媒充填室に、メツシユ状隔膜にて区
画し、レトルトの空気予熱室側端部には空気供給
源からの空気供給量を測定・制御する流量計を経
て、空気を空気予熱室に送給する空気送給管が連
結され、また、レトルト内触媒充填室には、加熱
炉の炉壁部に配設された断熱材を貫通して配管さ
れ、ブタン等の炭化水素ガス供給量を測定・制御
する流量計を経て、炉外配管によつて導かれた、
ブタン等の炭化水素ガス供給管が連結され、さら
にレトルトの触媒充填室側端部には、変成された
変成ガスを冷却するクーラーが連結された構造と
することにより、予熱された空気によつて、炭化
水素ガスを急速に加熱・混合させ、効率的に吸熱
型ガスを変成することのできることを特徴とし
た、吸熱型ガス変成装置によつて達成される。
ホ 実施例
以下、添付図面に基づいて、本発明の実施例を
説明する。
第２図に、本発明の吸熱型ガス変成装置の概略
図を示す、
なお、同実施例において、前記第１図の従来例
と、同一又は相当部分については、第１図と同一
の符号を付することにより説明を省略する。
また、この実施例では、炭化水素ガスとして、
ブタンに例をとつて説明する。
本発明の吸熱型ガス変成装置の構成は、第２図
から明らかなように、ブタン流量計４、空気流量
計５、空気予熱室６a′と触媒充填室６ｂが、メツ
シユ状隔膜６ｃによつて区画されたレトルト６、
触媒７、クーラ８、加熱炉９からなつている。
そして、従来の吸熱型ガス変成装置と異なる点
は、ブタン１の供給方法である。
本発明の吸熱型ガス変成装置では、空気予熱室
６a′において、930℃の高温に加熱した、空気２
の8.6／min中に、炉外配管によつて室温に保
持された、ブタン１の0.86／minを、加熱炉９
を貫通して配設された断熱材１０に穿設された孔
から供給し、触媒充填室６ｂにおいて、ブタン１
を急速に加熱した後、酸素過剰率を1.05として、
空気と混合させて、触媒により変成された組成を
下表に示す。
B. Field of Industrial Application The present invention relates to an endothermic gas conversion method and an apparatus thereof, and more particularly, to quenching and tempering of steel parts,
Alternatively, the present invention relates to an endothermic gas conversion method and apparatus for converting an endothermic gas used during heat treatment such as carburizing and quenching at a high temperature of 850 to 1100°C using a catalyst. B. Prior Art Endothermic chamber gas used during heat treatment such as hardening and tempering of steel parts or carburizing and quenching is conventionally produced by an endothermic chamber gas conversion device called a so-called RX gas generation furnace. This RX gas generating furnace supplies methane (CH 4 , propane (C 3 H 8 ), butane (C 4 H 10 ), etc. A mixed gas of hydrocarbon gas and air is supplied to convert the endothermic chamber gas, which contains CO, H 2 and N 2 as main components and trace amounts of CH 4 , H 2 O and C. Now, if we take butane as an example of a hydrocarbon gas and observe its modification reaction, the reaction C 4 H 10 +20 2 +7.52N 2 →4CO+5H+7.52N proceeds in the retort, and at this time, the following reaction occurs. Equilibrium reaction is maintained. H 2 +CO 2 CO + H 2 O CH 4 +CO 2 2CO + 2H 2 CH 4 +H 2 OCO + 3H 2 Therefore, between each component, CO≒23%, H 2 ≒29
%, CH 4 = trace ~ 0.2%, CO 2 = trace ~ 20%, balance N 2 in equilibrium with each other. When the mixing ratio of butane and air is changed, the equilibrium values of CH 4 , CO 2 , H 2 O, etc. change depending on the mixing ratio. By the way, in this conventional endothermic gas shift method, before the mixed gas of hydrocarbon gas and air contacts the catalyst and the shift reaction proceeds, the hydrocarbon gas thermally decomposes and generates soot C. , the equilibrium state is disrupted and equilibrium gas cannot be obtained, resulting in CO, CO 2
This has the disadvantage that it is difficult to control the carbon tension due to the Furthermore, there is a drawback that the soot (C) produced as described above adheres to the catalyst, resulting in a decrease in catalytic activity. To explain the above-mentioned drawbacks of the prior art based on a specific conventional device, in FIG.
When a mixed gas consisting of butane 1 at 0.86/min and air 2 at 8.6/min is fed to the retort 6 at 930°C, the endothermic chamber gas 3 is heated at 15/min under the catalyst 7 at 100 c.c. It is something that can be transformed. Here, in the conventional shift conversion method, in order to prevent thermal decomposition of the hydrocarbon gas in the retort 6, the rapid heating section 6a has a multi-tube structure consisting of several small diameter pipes, which easily absorbs heat from the heating furnace. In other words, in this rapid heating section 6a, the following thermal decomposition reaction of butane occurs: C 4 H 10 →C↓+2CH 4 +H 2 to produce soot (C). To suppress air,
It is necessary to rapidly heat the butane gas mixture. However, the retort 6 of the conventional endothermic gas shift converter
As mentioned above, although the multi-tube structure of small diameter pipes is considered to promote rapid heating, it has the disadvantage that the generation of soot (C) cannot be completely suppressed. C. Purpose of the Invention The present invention uses an endothermic gas used in an atmosphere for heat treatment of steel parts, etc., by directly mixing hydrocarbon gas at room temperature with air that has been preheated to a high temperature, thereby efficiently transferring the hydrocarbon gas. By heating and accelerating the heating rate of hydrocarbon gas, thermal decomposition of hydrocarbon gas can be reliably suppressed, and endothermic gas in an equilibrium state due to catalytic reaction can be efficiently transformed. The object of the present invention is to provide a method for converting type gas and an apparatus therefor. D. Structure of the Invention According to the present invention, a mixed gas of a hydrocarbon gas such as butane and air is supplied into a retort filled with a catalyst and maintained at a high temperature to generate an endothermic gas. An endothermic gas transformation method and apparatus for gas transformation, wherein the retort is divided into a preheating chamber and a catalyst filling chamber by a mesh-like diaphragm, and the air is preheated in the preheating chamber and then flows into the catalyst filling chamber. On the other hand, hydrocarbon gases such as butane are directly supplied to the furnace via piping outside the furnace without preheating, in order to prevent thermal decomposition of the hydrocarbon gases and to efficiently obtain equilibrium gas through metamorphic reactions. , an endothermic gas transformation characterized by rapidly heating and mixing hydrocarbon gas with preheated air by feeding it into a catalyst filling chamber, and bringing it into contact with a catalyst to transform it into an endothermic gas. The retort is arranged in a heating furnace, and the retort is divided into an air preheating chamber and a catalyst filling chamber filled with a catalyst by a mesh-like diaphragm, and the retort has an air preheating chamber side end. An air supply pipe that supplies air to the air preheating chamber is connected to the retort catalyst filling chamber via a flow meter that measures and controls the amount of air supplied from the air supply source. The gas is piped through the heat insulating material installed on the furnace wall of the furnace, and is guided through the outside piping through a flow meter that measures and controls the amount of hydrocarbon gas supplied, such as butane.
A hydrocarbon gas supply pipe such as butane is connected to the retort, and a cooler is connected to the end of the retort on the side of the catalyst filling chamber to cool the converted gas. This is achieved by an endothermic gas shift device that is capable of rapidly heating and mixing hydrocarbon gas to efficiently transform endothermic gas. E. Embodiments Hereinafter, embodiments of the present invention will be described based on the accompanying drawings. FIG. 2 shows a schematic diagram of the endothermic gas shift apparatus of the present invention. In the same embodiment, the same or equivalent parts as in the conventional example shown in FIG. 1 are designated by the same reference numerals as in FIG. The explanation will be omitted by attaching it. In addition, in this example, as a hydrocarbon gas,
This will be explained using butane as an example. As is clear from FIG. 2, the structure of the endothermic gas shift apparatus of the present invention is such that a butane flow meter 4, an air flow meter 5, an air preheating chamber 6a' and a catalyst filling chamber 6b are connected to each other by a mesh-like diaphragm 6c. compartmentalized retort 6,
It consists of a catalyst 7, a cooler 8, and a heating furnace 9. The difference from conventional endothermic gas shift equipment is the method of supplying butane 1. In the endothermic gas shift apparatus of the present invention, the air 2 heated to a high temperature of 930°C in the air preheating chamber 6a' is
During 8.6/min of heating furnace 9, 0.86/min of butane 1, which was maintained at room temperature by piping outside the furnace, was
In the catalyst filling chamber 6b, butane 1
After heating rapidly, with an oxygen excess ratio of 1.05,
The composition of the mixture mixed with air and modified by the catalyst is shown in the table below.
【表】
表から明らかなように、従来の吸熱型ガス変成
装置で変成された吸熱型ガス組成は、CO、およ
びH2が平衡吸熱ガス組成に比べ、低目の値であ
り、しかも、変成反応に伴ない、すす（Ｃ）の生
成が認められるのに対し、本発明の吸熱型ガス変
成装置によつて変成された吸熱型ガス組成は、ほ
ぼ、平衡吸熱型ガスに近似しており、しかも、変
成反応に伴なう、すす（Ｃ）の生成は認められな
い。
ヘ 発明の作用効果
以上により明らかなように、本発明にかかる吸
熱型ガス変成方法およびその装置によれば、鋼部
品の熱処理用雰囲気等に用いる吸熱型ガスを、予
め高温に加熱された空気に、直接、室温の炭化水
素ガスを混合させて、炭化水素ガスを伝熱効率よ
く加熱し、炭化水素ガスの加熱速度を速めること
によつて、炭化水素ガスの熱分解を確実に抑制で
き、しかも、触媒反応による平衡状態の吸熱型ガ
スを、効率よく変成することができる利点があ
る。[Table] As is clear from the table, the endothermic gas composition transformed by the conventional endothermic gas shift equipment has lower CO and H 2 values than the equilibrium endothermic gas composition, and While the formation of soot (C) is observed as a result of the reaction, the composition of the endothermic gas transformed by the endothermic gas shift device of the present invention is almost similar to that of the equilibrium endothermic gas, Moreover, no production of soot (C) accompanying the metamorphic reaction was observed. F. Effects of the Invention As is clear from the above, according to the endothermic gas transformation method and apparatus according to the present invention, the endothermic gas used in the heat treatment atmosphere of steel parts is converted into air preheated to a high temperature. By directly mixing hydrocarbon gas at room temperature, heating the hydrocarbon gas with high heat transfer efficiency, and increasing the heating rate of the hydrocarbon gas, thermal decomposition of the hydrocarbon gas can be reliably suppressed. There is an advantage that endothermic gas in an equilibrium state due to a catalytic reaction can be efficiently transformed.
第１図は、従来の吸熱型ガス変成装置の概略
図、第２図は、本発明の吸熱型ガス変成装置の概
略図である。
１……ブタン、２……空気、３……吸熱型ガ
ス、４……ブタン流量計、５……空気流量計、６
……レトルト、６ａ……急速加熱部、６a′……空
気予熱室、６ｂ……触媒充填室、６ｃ……メツシ
ユ状隔膜、７……触媒、８……クーラ、９……加
熱炉、１０……断熱材。
FIG. 1 is a schematic diagram of a conventional endothermic gas shift device, and FIG. 2 is a schematic diagram of an endothermic gas shift device of the present invention. 1... Butane, 2... Air, 3... Endothermic gas, 4... Butane flow meter, 5... Air flow meter, 6
...Retort, 6a... Rapid heating section, 6a'... Air preheating chamber, 6b... Catalyst filling chamber, 6c... Messy diaphragm, 7... Catalyst, 8... Cooler, 9... Heating furnace, 10 ...Insulation material.
Claims (1)
に、ブタン等の炭化水素ガスと空気との混合ガス
を供給して、吸熱型ガスを変成させる、吸熱型ガ
ス変成方法であつて、 上記レトルトを、予熱室と触媒充填室にメツシ
ユ状隔膜により区画して、空気は、予熱室にて予
熱された後、触媒充填室に送給され、一方、ブタ
ン等の炭化水素ガスは、炭化水素ガスの熱分解を
防止するとともに、変成反応により平衡ガスを効
率的に得られるように、炉外配管により、予熱す
ることなく、直接、触媒充填室に送給することに
より、予熱された空気によつて、炭化水素ガスを
急速に加熱・混合し、触媒と接触させて吸熱型ガ
スを変成することを特徴とした吸熱型ガス変成方
法。 ２ 触媒を充填し、高温に保持されたレトルト内
に、ブタン等の炭化水素ガスと空気との混合ガス
を供給して、吸熱型ガスを変成させる、吸熱型ガ
ス変成装置であつて、 上記レトルトは、加熱炉内に配設されるととも
に、該レトルト内を空気予熱室と触媒を充填した
触媒充填室に、メツシユ状隔膜にて区画し、レト
ルトの空気予熱室側端部には、空気供給源からの
空気供給量を測定・制御する流量計を経て、空気
を空気予熱室に送給する空気供給管が連結され、
また、レトルト内触媒充填室には、加熱炉の炉壁
部に配設された断熱材を貫通して配管され、ブタ
ン等の炭化水素ガス供給量を測定・制御する流量
計を経て、炉外配管によつて導かれた、ブタン等
の炭化水素ガス供給管が連結され、さらに、レト
ルトの触媒充填室側端部には、変成された変成ガ
スを冷却するクーラーが連結された構造とするこ
とにより、予熱された空気によつて、炭化水素ガ
スを急速に加熱・混合させ、効率的に吸熱型ガス
を変成することのできることを特徴とした、吸熱
型ガス変成装置。[Claims] 1. An endothermic gas transformation method in which a mixed gas of a hydrocarbon gas such as butane and air is supplied into a retort filled with a catalyst and maintained at a high temperature to transform an endothermic gas. The retort is divided into a preheating chamber and a catalyst filling chamber by a mesh-like diaphragm, and air is preheated in the preheating chamber and then fed to the catalyst filling chamber, while hydrocarbons such as butane In order to prevent thermal decomposition of hydrocarbon gases and to efficiently obtain equilibrium gas through a shift reaction, the gas is directly delivered to the catalyst filling chamber through piping outside the furnace without being preheated. An endothermic gas transformation method characterized by rapidly heating and mixing hydrocarbon gas with preheated air and bringing it into contact with a catalyst to transform endothermic gas. 2. An endothermic gas conversion device that transforms an endothermic gas by supplying a mixed gas of a hydrocarbon gas such as butane and air into a retort filled with a catalyst and maintained at a high temperature; is arranged in the heating furnace, and the inside of the retort is divided into an air preheating chamber and a catalyst filling chamber filled with catalyst by a mesh-like diaphragm, and an air supply is provided at the end of the retort on the air preheating chamber side. An air supply pipe that delivers air to the air preheating chamber is connected through a flow meter that measures and controls the amount of air supplied from the source.
In addition, piping is connected to the catalyst filling chamber in the retort by penetrating the heat insulating material installed on the furnace wall of the heating furnace. A hydrocarbon gas supply pipe such as butane guided by piping is connected to the retort, and a cooler is connected to the end of the retort on the catalyst filling chamber side to cool the transformed gas. An endothermic gas shift device characterized by being able to rapidly heat and mix hydrocarbon gas with preheated air to efficiently transform endothermic gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58190424A JPS6081002A (en) | 1983-10-12 | 1983-10-12 | Endothermic gas conversion process and its apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58190424A JPS6081002A (en) | 1983-10-12 | 1983-10-12 | Endothermic gas conversion process and its apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6081002A JPS6081002A (en) | 1985-05-09 |
| JPH0453804B2 true JPH0453804B2 (en) | 1992-08-27 |
Family
ID=16257900
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58190424A Granted JPS6081002A (en) | 1983-10-12 | 1983-10-12 | Endothermic gas conversion process and its apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6081002A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9023181B2 (en) * | 2011-03-25 | 2015-05-05 | The United States Of America, As Represented By The Secretary Of Agriculture | Fast pyrolysis catalytic cracking pipe for producing bio-oils |
-
1983
- 1983-10-12 JP JP58190424A patent/JPS6081002A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6081002A (en) | 1985-05-09 |
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