JPH0446179B2 - - Google Patents
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- Publication number
- JPH0446179B2 JPH0446179B2 JP59223889A JP22388984A JPH0446179B2 JP H0446179 B2 JPH0446179 B2 JP H0446179B2 JP 59223889 A JP59223889 A JP 59223889A JP 22388984 A JP22388984 A JP 22388984A JP H0446179 B2 JPH0446179 B2 JP H0446179B2
- Authority
- JP
- Japan
- Prior art keywords
- sample
- activated carbon
- minutes
- ppm
- 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
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 62
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 21
- 238000001035 drying Methods 0.000 claims description 12
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 10
- 239000007864 aqueous solution Substances 0.000 claims description 9
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 230000003472 neutralizing effect Effects 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 230000003647 oxidation Effects 0.000 description 10
- 238000007254 oxidation reaction Methods 0.000 description 10
- 238000012360 testing method Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000007789 gas Substances 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 229910002621 H2PtCl6 Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Landscapes
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Description
この発明は、空気のようなガス中に含まれてい
るCOをCO2に、室温でも高い効率で転換するこ
とができるCO転換触媒を製造する方法に関する
ものである。
COをCO2に転換するための触媒として、活性
炭に白金を担持させたものが知られている（たと
えば特公昭57−36014号公報）。この公知のCO転
換触媒は、適当な粒度の活性炭に必要に応じて塩
酸洗浄・乾燥などの前処理を施してから、塩化白
金酸（H2PtCl6・6H2Ｏ）水溶液で処理したのち
乾燥し、ついでKBH4などの水溶液で還元処理
し、水洗・乾燥を経て空気中で高温加熱処理する
ことによつて製造されている。しかしこのような
従来の方法で製造されたCO転換触媒は、CO転換
効率が充分でなく、またCO含有ガスの流速が速
くなると転換効率が急激に低下するという欠点を
有している。たとえば、SV5300hr-1のとき出口
のCO濃度が20ppmであつたものが、10600hr-1で
は、170ppm以上になるという例がある。
この発明は、従来の方法で製造されたCO転換
触媒よりも著しく高いCO転換効率を有するCO転
換触媒を製造する方法を提供することを目的とし
ている。
この発明方法によれば、まず、適当な粒度の活
性炭に、必要に応じて塩酸洗浄・乾燥などの前処
理を施してから、H2PtCl6・6H2Ｏ水溶液で処理
したのち、炭酸ソーダ（Na2CO3）水溶液で中和
するか又は加熱空気で乾燥し、これをKBH4また
はNaBH4水溶液で還元処理してから乾燥する。
次いで、還元処理・乾燥後の後処理として、過酸
化水素（H2O2）による酸化処理を施して、残存
する還元剤を分解する。この酸化処理は、還元処
理・乾燥後の触媒を、たとえば３％程度の濃度の
過酸化水素水中に入れ、室温で適当時間振とうす
ることによつて容易に行なうことができる。
酸化処理後に乾燥することによつて得られた
CO転換触媒は、実験の結果、酸化処理のかわり
に単なる加熱乾燥処理を施したものと比較してき
わめて高いCO転換率を有していることが確認さ
れた。ただしこのようなCO転換効率の向上効果
は、活性炭に担持されているPt量が所定の値以
上である場合に限つて得られる。すなわち活性炭
に対する白金（Pt）の担持量が約６mg／ｇ・活
性炭以下になるような含浸操作ではCO転換効率
の向上はほとんど認められない。好ましいPt担
持量は約６mg／ｇ・活性炭以上になるような含浸
操作である。また酸化処理を過酸化水素による酸
化以外の手段、たとえば空気中での高温加熱処理
によつて行なつてもCO転換効率は向上しない。
実施例 １
活性炭（第１炭素(株)製の商品名「BFG」）300
ｇを２の５％塩酸中に90℃で１時間浸漬したの
ち引き上げ、十分水洗したのち120℃で２時間乾
燥することによつて前処理を施した。
つぎにこの前処理した活性炭を、水1.5にH2
PtCl6・6H2O16.2ｇ（Pt分約6.10ｇ）を溶解した
溶液中に浸漬し、時々振とうしながら90℃に４時
間保持した。つぎにこの混合物中に、60ｇのNa2
CO3を900c.c.の水に溶解した溶液を室温で30分間
にわたつて攪拌しながら徐々に滴下し、ついで０
℃に冷却してから、10ｇのKBH4を1.5の水に
溶解した溶液を攪拌下で２時間にわたつて徐々に
滴下した。ついで固形物を吸引過し、10の温
水で洗浄したのち、120℃で２時間乾燥した。
この触媒をさらに３の３％過酸化水素水中に
入れ、室温で１時間振とうし、ついで20℃で２時
間乾燥させることによつて酸化処理して試料Ａを
得た。この触媒はPtを20.3mg／ｇ活性炭の割合で
含むような含有操作を経ている。
比較のために、H2PtCl6・6H2Ｏ水溶液として、
水1.5にH2PtCl6・6H2Ｏ 4.1ｇ（Pt分約1.50
ｇ）を使用した以外は試料Ａと同じ条件で得られ
た試料Ｂ（Ptは5.2mg／ｇ活性炭になるような含浸
操作である。以下同じ）と、さらに過酸化水素水
による酸化処理を省いた試料Ｃ（Ptは5.2mg／ｇ活
性炭）および試料Ｄ（Ptは20.3mg／ｇ活性炭）と
を用意した。
各試料Ａ、Ｂ、Ｃ、Ｄについてそれらの一部を
サンプルとしてとり、触媒活性試験を行ない、
CO転換効率を計測した。触媒活性試験は、図に
示す試験装置を用いて行なわれた。この試験装置
において、既知量のCOを含有する空気がバルブ
Ｖ１を通してサンプルガスホルダー１に導入さ
れ、ついでポンプＰ２の作用で、洗気ビン２およ
びフローメータ３を経て触媒部４に供給される。
この触媒部４は、内径17mm、高さ50mm（容積11.3
cm3）のもので、その中に被試験試料が充填され
る。触媒部４を通過したガスは、その一定量がバ
ルブＶ４を経て出口ガス分取容器５内に収容さ
れ、ポンプＰ３の作用で攪拌しながら一定時間貯
えられ、ついでバルブＶ５を経てCO分析器に送
られてCO含有量が計測される。
本発明にもとづく試料Ａの計測結果を下記の第
１表に示す（転換率は99.9％以上）。試料ガスは
湿潤空気中（乾燥空気ではない）に2360ppmの
COを添加したもので、触媒部４に室温で試料ガ
スがSV＝5000hr-1で流された。
The present invention relates to a method for producing a CO conversion catalyst that can convert CO contained in a gas such as air to CO 2 with high efficiency even at room temperature. As a catalyst for converting CO into CO2 , a catalyst in which platinum is supported on activated carbon is known (for example, Japanese Patent Publication No. 57-36014). This known CO conversion catalyst is made by pre-treating activated carbon with an appropriate particle size, such as washing with hydrochloric acid and drying as necessary, treating it with an aqueous solution of chloroplatinic acid (H 2 PtCl 6 6H 2 O), and then drying it. Then, it is manufactured by reducing it with an aqueous solution such as KBH 4 , washing with water, drying, and then heating it at high temperature in the air. However, the CO conversion catalyst produced by such a conventional method has the disadvantage that the CO conversion efficiency is not sufficient and the conversion efficiency rapidly decreases as the flow rate of the CO-containing gas increases. For example, there is an example where the CO concentration at the outlet was 20 ppm at SV 5300 hr -1 , but it increased to over 170 ppm at SV 10600 hr -1 . The present invention aims to provide a method for producing a CO conversion catalyst that has a significantly higher CO conversion efficiency than CO conversion catalysts produced by conventional methods. According to the method of this invention, activated carbon of an appropriate particle size is first pretreated with hydrochloric acid washing and drying as necessary, then treated with an aqueous solution of H 2 PtCl 6 .6H 2 O, and then treated with an aqueous solution of sodium carbonate ( Neutralize with an aqueous solution of Na 2 CO 3 or dry with heated air, reduce with a KBH 4 or NaBH 4 aqueous solution, and then dry.
Next, as a post-treatment after the reduction treatment and drying, an oxidation treatment with hydrogen peroxide (H 2 O 2 ) is performed to decompose the remaining reducing agent. This oxidation treatment can be easily carried out by placing the reduced and dried catalyst in a hydrogen peroxide solution having a concentration of about 3%, for example, and shaking it at room temperature for an appropriate period of time. Obtained by drying after oxidation treatment
As a result of experiments, it was confirmed that the CO conversion catalyst has an extremely high CO conversion rate compared to a catalyst that is simply heated and dried instead of oxidized. However, such an effect of improving CO conversion efficiency can be obtained only when the amount of Pt supported on activated carbon is a predetermined value or more. That is, in an impregnation operation in which the amount of platinum (Pt) supported on activated carbon is less than about 6 mg/g activated carbon, hardly any improvement in CO conversion efficiency is observed. A preferred impregnation operation is such that the amount of Pt supported is approximately 6 mg/g of activated carbon or more. Further, even if the oxidation treatment is performed by means other than oxidation using hydrogen peroxide, such as high-temperature heating treatment in air, the CO conversion efficiency does not improve. Example 1 Activated carbon (trade name “BFG” manufactured by Daiichi Carbon Co., Ltd.) 300
The sample was pretreated by immersing it in 5% hydrochloric acid (2) at 90°C for 1 hour, taking it out, thoroughly washing it with water, and drying it at 120°C for 2 hours. Next, add this pretreated activated carbon to 1.5 liters of water with H 2
It was immersed in a solution containing 16.2 g of PtCl 6 .6H 2 O (approximately 6.10 g of Pt) and kept at 90° C. for 4 hours with occasional shaking. Next, add 60g of Na 2 to this mixture.
A solution of CO 3 in 900 c.c. of water was gradually added dropwise with stirring at room temperature for 30 minutes, and then the temperature was reduced to 0.
After cooling to 0.degree. C., a solution of 10 g of KBH 4 in 1.5 parts of water was slowly added dropwise under stirring over a period of 2 hours. The solid matter was then filtered off by suction, washed with warm water for 10 minutes, and then dried at 120° C. for 2 hours. This catalyst was further oxidized by placing it in 3% hydrogen peroxide solution, shaking it at room temperature for 1 hour, and then drying it at 20°C for 2 hours to obtain Sample A. This catalyst underwent an operation to contain Pt at a ratio of 20.3 mg/g activated carbon. For comparison, as an aqueous solution of H 2 PtCl 6 6H 2 O,
4.1g of H2PtCl6・6H2O to 1.5% of water (Pt content approx. 1.50
Sample B was obtained under the same conditions as Sample A, except that Pt (Pt: 5.2 mg/g of activated carbon was used. The same applies hereinafter), and the oxidation treatment with hydrogen peroxide solution was omitted. Sample C (Pt: 5.2 mg/g activated carbon) and Sample D (Pt: 20.3 mg/g activated carbon) were prepared. A portion of each sample A, B, C, and D was taken as a sample and a catalytic activity test was conducted.
CO conversion efficiency was measured. The catalyst activity test was conducted using the test apparatus shown in the figure. In this test device, air containing a known amount of CO is introduced into the sample gas holder 1 through the valve V1 and then supplied to the catalyst section 4 via the air wash bottle 2 and the flow meter 3 under the action of the pump P2.
This catalyst section 4 has an inner diameter of 17 mm and a height of 50 mm (volume 11.3 mm).
cm 3 ) into which the test sample is filled. A certain amount of the gas that has passed through the catalyst section 4 is stored in the outlet gas separation container 5 via the valve V4, stored for a certain period of time while being stirred by the action of the pump P3, and then sent to the CO analyzer via the valve V5. The CO content will be measured. The measurement results of Sample A according to the present invention are shown in Table 1 below (conversion rate is 99.9% or more). The sample gas is 2360ppm in humid air (not dry air).
A sample gas containing CO was flowed through the catalyst section 4 at room temperature at SV=5000 hr -1 .
【表】
また比較例の試料Ｃについて同様の試験を行な
つた結果によれば（たゞし、入口CO濃度は
1590ppm）、同一条件で、開始から1.5分間の平均
CO濃度は700ppm（転換率56.0％）であり、６分
後には800ppmに上昇した。
さらに試料Ｂでは（入口CO濃度は1590ppm）、
開始から２分間の平均CO濃度は510ppm（転換率
68.01％）、3.5分後では412ppmであつた。
更に試料Ｄでは（入口CO濃度は2250ppm）、
SV5000hr-1の場合、10分間2ppm以下を保つてい
たが、SVを10000hr-1にすると22分後で110ppm、
32分後で400ppmに増加した。なお、その後、SV
を5000hr-1に減ずると、2ppm以下になつた。
試料ＢのCO転換率が、試料Ｃとくらべると、
時間の経過とともにやや回復しているのは、過酸
化水素水による酸化処理の効果であると推定され
るが、Ptの担持量が少ないために（Ptは5.2mg／
ｇ活性炭）、試料Ａ（Ptは20.3mg／ｇ活性炭）のよ
うな高いCO転換率は有していない。
本発明の試料Ａと比較例（H2O2酸化処理をし
ていない）の試料Ｄとをくらべると（Ptはいず
れも20.3mg／ｇ活性炭）、SV5000hr-1のときはい
ずれも2ppm以下であつたが、SVを10000hr-1に
すると、試料Ｄでは12分〜22分後で110ppm〜
400ppmに増加している。これに対して、H2O2酸
化処理をほどこした本発明の試料Ａでは、２分後
8ppm、10分後80ppmと、初期には一時的にやや
高くなる傾向があるものの、すぐに活性を回復し
て22分後ですでに2ppm以下となり、これを持続
している。すなわち、高いSVでもすぐれた活性
を示している。
実施例 ２
実施例１と同じ条件で前処理した活性炭30ｇ
を、水100c.c.にH2PtCl6・6H2Ｏ 1.0ｇ（Pt分約
0.38ｇ）を溶解した溶液中に浸漬し、時々振とう
しながら90℃に30分間保持し、ついで120℃で30
分間乾燥した。（Na2CO3による中和のかわりの、
加熱空気による乾燥処理）つぎに0.5ｇのNaBH4
を200c.c.の水に溶解した溶液中に浸漬して室温で
30分間静置し、吸引過後に水洗したのち、120
℃で30分間乾燥した。
さらにこの触媒を500c.c.の３％過酸化水素水中
に入れ、室温で１時間振とうし、ついで20℃で２
時間乾燥させることによつて酸化処理して試料Ｅ
（Ptは12.6mg／ｇ活性炭）を得た。
比較のために、H2O2による酸化処理のかわり
に、300℃で３時間高温空気で加熱して酸化した
以外は同じ操作を行なつて試料Ｆ（Ptは12.6mg／
ｇ活性炭）を得た。試料Ｅについて実施例１と同
様の触媒活性試験を行つた結果によれば
（SV5300hr-1、入口CO濃度2350ppm）、開始から
２分間の平均CO濃度は14ppm（転換率99.4％）
で、その経時変化は第２表のとおりであつた。[Table] Also, according to the results of a similar test on sample C as a comparative example (the inlet CO concentration was
1590ppm), average for 1.5 minutes from the start under the same conditions
The CO concentration was 700 ppm (conversion rate 56.0%) and rose to 800 ppm after 6 minutes. Furthermore, in sample B (inlet CO concentration is 1590 ppm),
The average CO concentration during the first 2 minutes was 510 ppm (conversion rate
68.01%) and 412 ppm after 3.5 minutes. Furthermore, in sample D (inlet CO concentration is 2250 ppm),
In the case of SV5000hr -1 , it was kept below 2ppm for 10 minutes, but when SV was set to 10000hr -1 , it became 110ppm after 22 minutes.
It increased to 400ppm after 32 minutes. Furthermore, after that, SV
When it was reduced to 5000hr -1 , it became less than 2ppm. When the CO conversion rate of sample B is compared with sample C,
It is presumed that the reason for the slight recovery over time is due to the effect of the oxidation treatment with hydrogen peroxide solution, but it is also due to the small amount of Pt supported (Pt is 5.2mg/
It does not have a high CO conversion rate like Sample A (Pt is 20.3 mg/g activated carbon). Comparing Sample A of the present invention with Sample D of the comparative example (no H 2 O 2 oxidation treatment) (Pt is 20.3 mg/g activated carbon in both cases), both are less than 2 ppm at SV5000hr -1 . However, when the SV is set to 10,000 hr -1 , sample D becomes 110 ppm after 12 to 22 minutes.
It has increased to 400ppm. On the other hand, in sample A of the present invention, which was subjected to H 2 O 2 oxidation treatment, after 2 minutes
8ppm, and 80ppm after 10 minutes, which tends to be a little high temporarily at the beginning, but the activity quickly recovers and after 22 minutes, it has already dropped to below 2ppm and continues to do so. In other words, it shows excellent activity even at high SV. Example 2 30g of activated carbon pretreated under the same conditions as Example 1
1.0g of H 2 PtCl 6・6H 2 O (approx. Pt) to 100c.c. of water.
0.38g) was dissolved in the solution, kept at 90°C for 30 minutes with occasional shaking, and then heated at 120°C for 30 minutes.
Dry for a minute. (Instead of neutralization with Na 2 CO 3 ,
(drying treatment with heated air) then 0.5 g of NaBH 4
at room temperature by immersing it in a solution of 200c.c. of water.
After leaving it for 30 minutes, washing with water after suction,
Dry for 30 minutes at °C. Further, this catalyst was placed in 500 c.c. of 3% hydrogen peroxide, shaken at room temperature for 1 hour, and then heated to 20°C for 2 hours.
Sample E was oxidized by drying for hours.
(Pt: 12.6 mg/g activated carbon) was obtained. For comparison, Sample F (Pt was 12.6 mg/kg) was prepared by performing the same procedure except that instead of oxidizing with H 2 O 2 , it was oxidized by heating in high-temperature air at 300°C for 3 hours.
g activated carbon) was obtained. According to the results of the same catalytic activity test as in Example 1 for Sample E (SV5300hr -1 , inlet CO concentration 2350ppm), the average CO concentration during the first 2 minutes was 14ppm (conversion rate 99.4%).
The changes over time were as shown in Table 2.
【表】
また比較試料Ｆについての同条件下の試験で
は、初期２分間の平均CO濃度は482ppm（転換率
79.5％）で、CO濃度は１分後で35ppm、12分後
で1760ppmであつた。
実施例 ３
活性炭300ｇについて、試料Ａと同様の処理を
行なつた。ただし、前処理に引きつづいて行なう
白金担持処理で使用した塩化白金酸（H2PtCl6・
6H2Ｏ）の量は5.5ｇ（Pt2.07ｇ）であり、H2O2
酸化処理では、３％のH2O2水を３使用した。
これを試料Ｇとし、H2O2処理をしないものを試
料Ｈとした。いずれもPtは6.7mg／ｇ活性炭であ
る。
実施例１と同様の触媒活性試験では
（SV5000hr-1、入口CO濃度はいずれも２，
510ppm）、試料Ｇの場合、６分後で出口のCO濃
度は18ppm、15分後で24ppm、30分後で43ppmで
あつた。これに比して、試料Ｈは５分後に
67ppm、10分後に110ppmとなり、本発明による
試料Ｇがはるかに高い効率を示した。
最後にPt量の影響を再度検討してみると、試
料Ａ（Ptは20.3mg／ｇ活性炭）、試料Ｅ（12.6mg／
ｇ活性炭）、試料Ｇ（6.9mg／ｇ活性炭）試料Ｂ
（5.2mg／ｇ活性炭）の順にPt量が少なくなり、そ
れにともなつて、初期のCO出濃度は、それぞれ
2ppm以下、4ppm、18ppm、510ppmと多くなる
が、6.9mg／ｇ活性炭までは18ppmと実用的なの
に対して、5.2mg／ｇ活性炭になると出口CO濃度
は510ppmと急増する。従つて、本発明における
Pt担持量は６mg／ｇ活性炭以上になるような操
作が必要である。[Table] In addition, in a test under the same conditions for comparative sample F, the average CO concentration during the initial 2 minutes was 482 ppm (conversion rate
79.5%), and the CO concentration was 35 ppm after 1 minute and 1760 ppm after 12 minutes. Example 3 300 g of activated carbon was treated in the same manner as Sample A. However, chloroplatinic acid (H 2 PtCl 6 .
6H 2 O) is 5.5 g (Pt2.07 g), H 2 O 2
In the oxidation treatment, 3% H 2 O 2 water was used.
This was designated as Sample G, and the one not subjected to H 2 O 2 treatment was designated as Sample H. In both cases, Pt was 6.7 mg/g activated carbon. In the same catalyst activity test as in Example 1 (SV5000hr -1 , inlet CO concentration was 2,
In the case of sample G, the CO concentration at the outlet was 18 ppm after 6 minutes, 24 ppm after 15 minutes, and 43 ppm after 30 minutes. In contrast, sample H was released after 5 minutes.
67 ppm, 110 ppm after 10 minutes, sample G according to the invention showed much higher efficiency. Finally, when we reexamined the effect of Pt amount, we found that sample A (Pt was 20.3 mg/g activated carbon) and sample E (12.6 mg/g activated carbon).
g activated carbon), sample G (6.9 mg/g activated carbon) sample B
(5.2 mg/g activated carbon), the amount of Pt decreases, and the initial CO output concentration decreases, respectively.
The CO concentration increases to 2ppm or less, 4ppm, 18ppm, and 510ppm, but up to 6.9mg/g activated carbon, it is practical at 18ppm, but when it reaches 5.2mg/g activated carbon, the outlet CO concentration rapidly increases to 510ppm. Therefore, in the present invention
It is necessary to operate so that the amount of Pt supported is 6 mg/g or more on activated carbon.
図はこの発明の実施例で使用された触媒活性試
験装置の系統図である。
The figure is a system diagram of a catalyst activity testing apparatus used in an example of the present invention.
Claims (1)
ち、炭酸ソーダ水溶液で中和するか又は加熱空気
で乾燥し、これを還元処理してから乾燥すること
により、活性炭に対して少なくとも６mg／ｇ・活
性炭の白金を担持させるような操作をほどこし、
ついで過酸化水素水を接触させることを特徴とす
るCO転換触媒の製造方法。1. After impregnating activated carbon with an aqueous solution of chloroplatinic acid, neutralizing it with an aqueous solution of sodium carbonate or drying it with heated air, reducing it and then drying it, the activated carbon has a concentration of at least 6 mg/g of activated carbon. The process is carried out in such a way that it supports platinum.
A method for producing a CO conversion catalyst, which comprises then contacting with a hydrogen peroxide solution.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59223889A JPS61103543A (en) | 1984-10-26 | 1984-10-26 | Preparation of co conversion catalyst |
| DE19853537894 DE3537894A1 (en) | 1984-10-26 | 1985-10-24 | METHOD FOR PRODUCING A CARBON MONOXIDE CONVERSION CATALYST |
| GB08526244A GB2166061B (en) | 1984-10-26 | 1985-10-24 | Process for preparing carbon monoxide conversion catalyst |
| US06/791,393 US4652537A (en) | 1984-10-26 | 1985-10-25 | Process for preparing carbon monoxide platinum conversion catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59223889A JPS61103543A (en) | 1984-10-26 | 1984-10-26 | Preparation of co conversion catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61103543A JPS61103543A (en) | 1986-05-22 |
| JPH0446179B2 true JPH0446179B2 (en) | 1992-07-29 |
Family
ID=16805293
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59223889A Granted JPS61103543A (en) | 1984-10-26 | 1984-10-26 | Preparation of co conversion catalyst |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61103543A (en) |
-
1984
- 1984-10-26 JP JP59223889A patent/JPS61103543A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61103543A (en) | 1986-05-22 |
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