JPS63159210A - Decomposition of carbon dioxide gas - Google Patents
Decomposition of carbon dioxide gasInfo
- Publication number
- JPS63159210A JPS63159210A JP62037729A JP3772987A JPS63159210A JP S63159210 A JPS63159210 A JP S63159210A JP 62037729 A JP62037729 A JP 62037729A JP 3772987 A JP3772987 A JP 3772987A JP S63159210 A JPS63159210 A JP S63159210A
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- dioxide gas
- carbon
- gas
- reaction
- 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.)
- Pending
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 23
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 22
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 9
- 239000007789 gas Substances 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 20
- 229910001868 water Inorganic materials 0.000 claims abstract description 13
- 238000000034 method Methods 0.000 claims abstract description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000001257 hydrogen Substances 0.000 claims abstract description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 6
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims abstract description 3
- 239000000203 mixture Substances 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 35
- 150000002431 hydrogen Chemical class 0.000 description 4
- 230000000694 effects Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は炭酸ガスの分解方法に関し、特に宇宙船、宇宙
基地等の有人又は生物塔載の宇宙航行体、長期間潜航型
潜水艦、深海作業船等での環境制御に有利に適用しつる
炭酸ガス分解方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for decomposing carbon dioxide gas, and is particularly applicable to manned or biological space vehicles such as spacecraft and space bases, long-term submersible submarines, and deep-sea operations. This invention relates to a carbon dioxide decomposition method that can be advantageously applied to environmental control on ships and the like.
炭酸ガスと水素を反応させ炭素と水を生成するボッシュ
反応は、次の単一反応式
０式％（１）
で表わされると言われ、単一の反応として一つの反応器
、一つの反応条件で従来より実施さｎていた。The Bosch reaction, in which carbon dioxide gas and hydrogen react to produce carbon and water, is said to be expressed by the following single reaction equation (1), and requires only one reactor and one reaction condition as a single reaction. This has traditionally been done in the past.
従来、上記（１１式で表わされる反応として、単一の反
応器にて反応させた場合、反応効率が低く、ｃｏ の
副生が多くみられた。従って、上記反応効率の低さによ
り、反応器全体の容量が大型化あるいは低い被処理ガス
流量しか得られないという問題があり、かかるボッシュ
反応を利用した装置の産業上の利用分野を著じるしく制
限していた。Conventionally, when the above reaction (expressed by formula 11) was carried out in a single reactor, the reaction efficiency was low and a large amount of co was produced as a by-product. Therefore, due to the low reaction efficiency, the reaction There are problems in that the capacity of the entire device becomes large or only a low flow rate of the gas to be processed can be obtained, which significantly limits the industrial field of application of devices that utilize the Bosch reaction.
本発明はかかる従来技術の欠点を解消した炭酸ガスの分
解方法を提供することを目的とする。An object of the present invention is to provide a method for decomposing carbon dioxide gas that eliminates the drawbacks of the prior art.
本発明は炭酸ガスに水素を作用させて炭素と水に分解す
る方法において、異なる２つの温度帯域をもつ炭酸ガス
分解触媒充填部に炭酸ガスと水素との混合ガスを供給し
、第１の温度帯域で炭酸ガスを一酸化炭素と水とに分解
し、第２の温度帯域で前記第１の温度帯域で生成した一
酸化炭素を炭素と水とに分解することを特徴とする炭素
ガスの分解方法に関する。The present invention is a method of decomposing carbon dioxide gas into carbon and water by acting hydrogen on it, in which a mixed gas of carbon dioxide gas and hydrogen is supplied to a carbon dioxide gas decomposition catalyst filling section having two different temperature zones, and a first temperature Decomposition of carbon gas, characterized in that carbon dioxide gas is decomposed into carbon monoxide and water in a zone, and carbon monoxide generated in the first temperature zone is decomposed into carbon and water in a second temperature zone. Regarding the method.
本発明者らは、上記従来技術の問題点を解決する丸めに
、温度条件や原料ガスの種類を、種々変化させ実験を行
ったところ、前記（１）式で示される反応は、下記（２
１式と（３）式の２段階に分れて進行しているものであ
夛、シかも夫々異なる最適反応温度をもつことを見い出
した。In order to solve the problems of the prior art described above, the present inventors conducted experiments by varying the temperature conditions and the type of raw material gas, and found that the reaction represented by the above equation (1) is as follows (2
It has been found that the reaction proceeds in two stages, Equation 1 and Equation (3), and that each has a different optimum reaction temperature.
Ｃｏ２＋）Ｉ２→Ｃｏ ＋Ｈ２０（２）Ｇｏ ＋Ｈ４０
＋Ｈ，０１３１
すなわち、上記１２１式で示される反応温度帯域は９０
０Ｃ以上であり、上記１３１式で示される反応温度帯域
は、６００〜６５０Ｃに最適温度をもつことが判明しな
。また、この時の供給ガス中の００２とＨ２の比率は１
：２が最適であることが同時に判明した。Co2+)I2→Co +H20(2)Go +H40
+H,0131 That is, the reaction temperature range shown by the above formula 121 is 90
0C or more, and it has been found that the reaction temperature range shown by the above formula 131 has an optimum temperature in the range of 600 to 650C. Also, the ratio of 002 and H2 in the supplied gas at this time is 1
:2 was also found to be optimal.
そこで、炭酸ガス分解触媒充填部を上記の異なる温度帯
域になるように維持し、先ず（１１式で表わされる反応
をその最適温度範囲内の？００Ｃで行わせ、次に（２）
式で表わされる反応をごの最適温度範囲内の６３０Ｃで
行わせると、従来の反応効率が１８Ｘであつ九のに比較
し、本発明による２段反応方式では、反応効率が２５％
に増加した。Therefore, the carbon dioxide gas decomposition catalyst packed part is maintained in the different temperature ranges mentioned above, and the reaction expressed by (11) is first carried out at -00C within its optimum temperature range, and then (2)
When the reaction represented by the formula is carried out at 630C, which is within the optimum temperature range, the reaction efficiency is 18X compared to that of the conventional method, and the reaction efficiency of the two-stage reaction method according to the present invention is 25%.
increased to
なお、上述の反応を実施するにあたっては、触媒として
Ｆｅ又はＮｚのワイヤ状触媒を用いた。In carrying out the above-mentioned reaction, a wire-shaped Fe or Nz catalyst was used as the catalyst.
このように、本発明では、上記（２）、（３１式の反応
を夫々、最適温度条件下にて実施することにより、反応
効率を最大にすることを特徴とするものである。As described above, the present invention is characterized by maximizing the reaction efficiency by carrying out the reactions of formulas (2) and (31) above under optimal temperature conditions, respectively.
次に、本発明による炭酸ガスの分解方法の第１の実施頭
株を第１図に基づき説明する。この態様は１個の反応器
に２つの異なった温度帯域を設けた例である。Next, a first embodiment of the method for decomposing carbon dioxide according to the present invention will be explained based on FIG. This embodiment is an example in which one reactor is provided with two different temperature zones.
第１図において４は反応器であり、この反応器４内には
反応を促進する九めの触媒５（例えば、Ｆｅ又はＮ１の
ワイヤ状触媒）が充填されている。この触媒３を充填し
た層は、第１段電気ヒータ５、第２段電気ヒータ６によ
って前記（２）、１３１式で示される夫々の反応が効率
よく進行する温度（すなわち、Ｃ２）式の反応に対して
は９００Ｃ以上、最適には９００ｔＺ’、＋３１式の反
応に対しては６００〜６５０ Ｃ，最適には６３ｏｃ）
に夫々調節することによシ、触媒３の充填層に熱勾配を
与える。In FIG. 1, 4 is a reactor, and this reactor 4 is filled with a ninth catalyst 5 (eg, Fe or N1 wire-shaped catalyst) for promoting the reaction. The layer filled with this catalyst 3 is heated to a temperature at which each reaction shown in the above-mentioned equations (2) and 131 proceeds efficiently (i.e., C2) by the first-stage electric heater 5 and the second-stage electric heater 6. 900C or higher for the reaction, optimally 900tZ', 600-650C for the +31 reaction, optimally 63oc)
A thermal gradient is imparted to the packed bed of the catalyst 3 by adjusting the respective values.
ここで、あらかじめ水素（Ｈ２）ガスと混合された被処
理ガス１ （Ｃｏ２＋ Ｆｌ、） （混合比は１：２
）は、反応器内の触媒３の充填層上部〜中部にて前記（
２１式の反応後、引き続き触媒３の充填層中部〜下部に
て前記（３１式の反応が進行する。Here, the gas to be treated 1 (Co2+ Fl,) is mixed with hydrogen (H2) gas in advance (mixing ratio is 1:2).
) is the above (
After the reaction of formula 21, the reaction of formula 31 proceeds in the middle to lower part of the packed bed of catalyst 3.
反応器４から放出された処理ガス中には、ＣＯ２及びＣ
Ｏ成分を含む九め、循環ガス２として反応器４の入口へ
と循環される。この（３１式の反応にて生成した遊離炭
素（Ｃ）は固体として反応器４内の主として触媒５の充
填層中にとどまる。また、同様に生成し念水分（Ｈ，Ｏ
）は、連続的に凝縮器７にてドレン配管８より排出され
る。The process gas released from the reactor 4 contains CO2 and C
The gas containing the O component is recycled to the inlet of the reactor 4 as a circulating gas 2. The free carbon (C) produced in the reaction of (Equation 31) remains as a solid mainly in the packed bed of the catalyst 5 in the reactor 4.
) is continuously discharged from the drain pipe 8 in the condenser 7.
本発明の他の実施態様を第２図に基づき説明する。この
態様は２個の反応器を用い夫々の反応器を異った温度帯
域に維持した例である。Another embodiment of the present invention will be described based on FIG. This embodiment is an example in which two reactors are used and each reactor is maintained in a different temperature range.
第２図において、４．６は夫々第１段、第２段反応器で
あり、夫々の反応器内には反応を促進するための触媒が
触媒充填層５，７に充填されている。さらに電気ヒータ
８，９によって第１段４及び第２段反応器６は反応効率
が最高となるように夫々、最適な温度に調節される。In FIG. 2, numerals 4 and 6 denote first and second stage reactors, respectively, and catalyst packed beds 5 and 7 are filled with a catalyst to promote the reaction in each reactor. Further, electric heaters 8 and 9 adjust the temperatures of the first stage 4 and second stage reactor 6 to optimal temperatures, respectively, so that the reaction efficiency is maximized.
（例えば第１段は９００Ｃ，第２段は６３０ Ｃ）ここ
であらかじめ水素（Ｈ２）ガスと混合された被処理ガス
１ （Ｃｏ２＋ ！（２） は、第１段反応器４内の
触媒充填層５で前記（２）式の反応後、さらに第２段反
応器６へと導かれる。ＣＯ，成分が減少し、００ 成分
が増加した被処理ガス２は第２段反応器６の触媒充填７
１７で前記（３１式の反応が進行する。(For example, the first stage is 900C, the second stage is 630C) Here, the to-be-treated gas 1 (Co2+!(2)) mixed with hydrogen (H2) gas in advance is transferred to the catalyst packed bed in the first stage reactor 4. After the reaction of formula (2) in step 5, the gas is further guided to the second stage reactor 6.The gas to be treated 2, in which the CO and components have decreased and the 00 component has increased, is sent to the catalyst filling 7 of the second stage reactor 6.
In 17, the reaction of formula 31 proceeds.
第２段反応器６から放出された処理ガス中には、 ＣＯ
２及びＣＯ成分を含むため循環ガス３として第１段反応
器４人口へと循環させられる。The process gas released from the second stage reactor 6 contains CO
Since it contains 2 and CO components, it is circulated as a circulating gas 3 to the first stage reactor 4.
なお、前記（２１％（３１式の反応にて生成し九遊離炭
素（Ｃ１は固体として反応器内４，６の触媒充填層５，
７中にとどまる。また、同様に生成し九水分（Ｈ２Ｏ）
Ｆｉ連続的に凝縮器１１によってドレン配管１０より
系外へ排出する。In addition, the above (21% (9 free carbon produced in the reaction of formula 31) (C1 is a solid in the catalyst packed bed 5 in the reactor 4, 6,
Stay inside 7. Additionally, nine water (H2O) is produced in the same way.
The Fi is continuously discharged from the system through the drain pipe 10 by the condenser 11.
なお、第１段反応器４、第２段反応器６には、夫々温度
センナ（図示せず）を配置し、ヒータ８．９と共に制御
装置（図示せず）により最適な温度条件にコントロール
するようにすのがよい。In addition, a temperature sensor (not shown) is arranged in each of the first stage reactor 4 and the second stage reactor 6, and the temperature is controlled to the optimum temperature condition by a controller (not shown) together with a heater 8.9. It is better to do so.
本発明によシ、前記（２）、（３１式で示される反応を
最適条件下にて実施することが可能となる。According to the present invention, it becomes possible to carry out the reactions shown in formulas (2) and (31) under optimal conditions.
このことＫよシ、反応器全体の設備規模は、従来のもの
と比較して約％と小型化することが可能となり、よシ広
い産業上の利用分野への適用を可能にすることができた
。As a result, the overall equipment scale of the reactor can be reduced by approximately % compared to conventional reactors, making it possible to apply it to a wider range of industrial applications. Ta.
第１図及び第２図は、本発明を実施する念めのフローを
示す。1 and 2 show a preliminary flow for implementing the present invention.
Claims (1)
おいて、異なる２つの温度帯域をもつ炭酸ガス分解触媒
充填部に炭酸ガスと水素との混合ガスを供給し、第１の
温度帯域で炭酸ガスを一酸化炭素と水とに分解し、第２
の温度帯域で前記第１の温度帯域で生成した一酸化炭素
を炭素と水とに分解することを特徴とする炭素ガスの分
解方法。In a method of decomposing carbon dioxide gas into carbon and water by acting hydrogen on it, a mixed gas of carbon dioxide gas and hydrogen is supplied to a carbon dioxide gas decomposition catalyst packed part that has two different temperature zones, and carbon dioxide gas is decomposed in the first temperature zone. The gas is decomposed into carbon monoxide and water, and the second
A method for decomposing carbon gas, comprising decomposing carbon monoxide generated in the first temperature range into carbon and water in the temperature range.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19797986 | 1986-08-22 | ||
| JP61-197979 | 1986-12-23 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63159210A true JPS63159210A (en) | 1988-07-02 |
Family
ID=16383497
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62037729A Pending JPS63159210A (en) | 1986-08-22 | 1987-02-23 | Decomposition of carbon dioxide gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63159210A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0945402A1 (en) * | 1998-03-25 | 1999-09-29 | Research Institute of Innovative Technology for the Earth | Method for producing carbon |
| JP2006027949A (en) * | 2004-07-15 | 2006-02-02 | Electric Power Dev Co Ltd | Method of using carbon oxide-containing gas |
| JP4598994B2 (en) * | 2000-06-30 | 2010-12-15 | 三菱重工業株式会社 | Carbon dioxide reduction equipment |
| JP2015514670A (en) * | 2012-04-16 | 2015-05-21 | シーアストーン リミテッド ライアビリティ カンパニー | Method and system for capturing and sequestering carbon and reducing the mass of carbon oxide in a waste gas stream |
| JP2015514669A (en) * | 2012-04-16 | 2015-05-21 | シーアストーン リミテッド ライアビリティ カンパニー | Method for producing solid carbon by reducing carbon dioxide |
-
1987
- 1987-02-23 JP JP62037729A patent/JPS63159210A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0945402A1 (en) * | 1998-03-25 | 1999-09-29 | Research Institute of Innovative Technology for the Earth | Method for producing carbon |
| JP4598994B2 (en) * | 2000-06-30 | 2010-12-15 | 三菱重工業株式会社 | Carbon dioxide reduction equipment |
| JP2006027949A (en) * | 2004-07-15 | 2006-02-02 | Electric Power Dev Co Ltd | Method of using carbon oxide-containing gas |
| JP2015514670A (en) * | 2012-04-16 | 2015-05-21 | シーアストーン リミテッド ライアビリティ カンパニー | Method and system for capturing and sequestering carbon and reducing the mass of carbon oxide in a waste gas stream |
| JP2015514669A (en) * | 2012-04-16 | 2015-05-21 | シーアストーン リミテッド ライアビリティ カンパニー | Method for producing solid carbon by reducing carbon dioxide |
| JP2018104282A (en) * | 2012-04-16 | 2018-07-05 | シーアストーン リミテッド ライアビリティ カンパニー | Method for producing solid carbon by reducing carbon dioxide |
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