JPH08332392A - Oxidation catalyst of un-burnt hydrocarbon in exhaust gas and removing method thereof - Google Patents
Oxidation catalyst of un-burnt hydrocarbon in exhaust gas and removing method thereofInfo
- Publication number
- JPH08332392A JPH08332392A JP7167955A JP16795595A JPH08332392A JP H08332392 A JPH08332392 A JP H08332392A JP 7167955 A JP7167955 A JP 7167955A JP 16795595 A JP16795595 A JP 16795595A JP H08332392 A JPH08332392 A JP H08332392A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- catalyst
- platinum
- palladium
- supported
- 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.)
- Granted
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 95
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 58
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 58
- 230000003647 oxidation Effects 0.000 title claims abstract description 30
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 30
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title claims description 16
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 102
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000007789 gas Substances 0.000 claims abstract description 67
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 49
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 47
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 30
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000001301 oxygen Substances 0.000 claims abstract description 26
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 26
- 230000001590 oxidative effect Effects 0.000 claims abstract description 9
- 239000000758 substrate Substances 0.000 claims description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- 229910052878 cordierite Inorganic materials 0.000 claims description 9
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 claims description 9
- 238000011068 loading method Methods 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 abstract 1
- 229910052782 aluminium Inorganic materials 0.000 abstract 1
- 238000012360 testing method Methods 0.000 description 24
- 239000010410 layer Substances 0.000 description 21
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 13
- 239000007900 aqueous suspension Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 239000002737 fuel gas Substances 0.000 description 7
- 239000011248 coating agent Substances 0.000 description 6
- 238000000576 coating method Methods 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000010948 rhodium Substances 0.000 description 4
- 239000011247 coating layer Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- -1 etc. Substances 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 238000010304 firing Methods 0.000 description 3
- 229910010272 inorganic material Inorganic materials 0.000 description 3
- 239000011147 inorganic material Substances 0.000 description 3
- 238000011056 performance test Methods 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000004453 electron probe microanalysis Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 229910052703 rhodium Inorganic materials 0.000 description 2
- 239000000523 sample Substances 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical class [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910000599 Cr alloy Inorganic materials 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 150000001242 acetic acid derivatives Chemical class 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000004703 alkoxides Chemical class 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 239000000788 chromium alloy Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000036962 time dependent Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、排ガス中の低濃度（未
燃焼）炭化水素用酸化触媒及びその除去方法に関し、よ
り詳しくはハニカム基材にＰｔとＰｄとを混在させて担
持させ、両金属の担持量をこれまで有効な量として知ら
れていた範囲より多く且つ特定範囲で担持させてなる、
有効な炭化水素酸化能を備え、優れた耐久性を有する酸
素過剰な排ガス中の低濃度焼炭化水素用酸化触媒及びこ
の触媒を使用して酸素過剰で低濃度炭化水素を含む排ガ
ス中の炭化水素を酸化し、除去する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an oxidation catalyst for low-concentration (unburned) hydrocarbons in exhaust gas and a method for removing the same. More specifically, Pt and Pd are mixed and supported on a honeycomb substrate, The amount of metal carried is greater than the range known as an effective amount up to now and is carried in a specific range,
Oxidation catalyst for low-concentration burned hydrocarbon in exhaust gas with excess oxygen, which has effective hydrocarbon oxidizing ability and excellent durability, and hydrocarbon in exhaust gas containing low-concentration hydrocarbon with excess oxygen using this catalyst To oxidize and remove.
【０００２】[0002]
【従来の技術】自動車、航空機、火力発電、各種工場等
から排出される排ガスにはＮＯｘやＳＯｘ、或いは臭気
物質、ばいじん等のほか、未燃焼の炭化水素（ＨＣ）が
含有されている。また産業廃棄物、都市ゴミ等の焼却時
においては、それら廃棄物の由来や組成如何等にもよる
が、それら物質に加え、塩化水素ガス等が生成する。こ
のためこれらを含む排ガスに対して種々の対策が採ら
れ、さらに研究、開発が進められており、そしてこの点
はガスエンジン、ガスタ−ビン等を使用するコ−ジェネ
レ−ションシステムから排出される排ガスについても同
様である。Exhaust gas emitted from automobiles, aircraft, thermal power generation, various factories, etc. contains NOx and SOx, odorous substances, dust and the like, as well as unburned hydrocarbons (HC). When incinerating industrial waste, municipal waste, etc., hydrogen chloride gas and the like are produced in addition to these substances, depending on the origin and composition of the waste. For this reason, various measures have been taken against exhaust gas containing these, and further research and development have been advanced, and this point is emitted from cogeneration systems using gas engines, gas turbines, etc. The same applies to exhaust gas.
【０００３】従来、ガスエンジン、ガスタ−ビン、ボイ
ラ−、或いは加熱炉などでは、燃料ガスとして都市ガス
その他、メタン、エタン、プロパン、ブタン等を含む燃
料ガスが使用されているが、その燃焼効率や熱効率を高
めるために空気比すなわち燃料ガスに対する空気の比率
を燃料ガスリ−ン（ｌｅａｎ）側、すなわち燃料ガスに
対して空気量を燃料ガスの完全燃焼に必要な理論空気量
の１．０〜５．０倍、特に１．０〜３．０倍とするいわ
ゆる希薄燃焼方式が適用されてきている。Conventionally, in a gas engine, a gas turbine, a boiler, a heating furnace, etc., city gas and other fuel gas containing methane, ethane, propane, butane, etc. have been used as the fuel gas. In order to improve the thermal efficiency, the air ratio, that is, the ratio of air to fuel gas, is set to the fuel gas lean side, that is, the air amount to the fuel gas is 1.0 to the theoretical air amount necessary for complete combustion of the fuel gas. A so-called lean burn method has been applied, which is 5.0 times, particularly 1.0 to 3.0 times.
【０００４】そしてこれらの点は、単一の駆動源（エネ
ルギ−源）から電力、機械エネルギ−及び熱エネルギ−
を生産し、エネルギ−を高効率に利用可能とするいわゆ
るコ−ジェネレ−ションシステムにおける希薄燃焼ガス
エンジンについても同様である。しかしそのような希薄
燃焼方式の場合には、その排ガス中に少量の低級炭化水
素（特にメタン）、窒素酸化物（ＮＯｘ）、一酸化炭素
等とともに、多量の酸素及び水蒸気が共存することにな
る。[0004] These points are derived from a single driving source (energy source) to electric power, mechanical energy and thermal energy.
The same applies to a lean burn gas engine in a so-called cogeneration system that produces high efficiency and can use energy with high efficiency. However, in the case of such a lean burn system, a large amount of oxygen and water vapor coexist in the exhaust gas together with a small amount of lower hydrocarbons (especially methane), nitrogen oxides (NOx), carbon monoxide and the like. .
【０００５】ところで、これまで特に炭化水素（ＨＣ）
を微量含む（例えば５０００ｐｐｍ程度以下）燃焼排ガ
ス中のＨＣを酸化し除去する手法としては、排ガス中の
３成分（ＨＣ、ＣＯ、ＮＯｘ）を同一触媒で浄化するい
わゆる三元触媒による処理法が開発され、その一部は実
用化されてきている。この触媒は例えばＰｔ、Ｐｄ、Ｒ
ｈ等の貴金属をアルミナ等の担体に対して０．１〜３ｇ
／ｌ程度担持させたもので、この触媒に上記排ガスを例
えば温度５００〜７００℃程度の条件下で通して処理す
ることにより、その排ガス中のＮＯｘ、ＣＯ及びＨＣを
同時に除去するものである。By the way, especially hydrocarbons (HC)
As a method to oxidize and remove HC in combustion exhaust gas containing a trace amount (for example, about 5000 ppm or less), a so-called three-way catalyst treatment method for purifying three components (HC, CO, NOx) in exhaust gas with the same catalyst has been developed. However, some of them have been put to practical use. This catalyst is, for example, Pt, Pd, R
0.1 to 3 g of precious metal such as h with respect to a carrier such as alumina
In this case, NOx, CO, and HC in the exhaust gas are simultaneously removed by treating the catalyst with the exhaust gas passing through the catalyst under conditions of a temperature of 500 to 700 ° C., for example.
【０００６】しかし、三元触媒による処理法では、燃料
ガスに対し理論空気比に近い条件（空気比が１．０付
近）で燃焼され、酸素が殆んど存在しない排ガスに対し
てしか有効に適用することはできず、酸素過剰で且つ排
ガス中のＨＣ成分がとりわけメタンである条件下では有
効に作用しない。また酸化触媒としてＰｔやＰｄを単独
で使用するＰｔ／Ａｌ2Ｏ3やＰｄ／Ａｌ2Ｏ3等がある
が、これらは有機溶剤やＣＯの酸化触媒としては有効で
あるが、そのようなＰｔやＰｄの単独触媒ではメタンの
酸化除去には有効に作用しない。However, in the treatment method using a three-way catalyst, the fuel gas is burned under conditions close to the theoretical air ratio (air ratio is about 1.0), and is effective only for exhaust gas in which oxygen is almost absent. It cannot be applied and does not work effectively under conditions of excess oxygen and especially where the HC component in the exhaust gas is methane. Further, there are Pt / Al 2 O 3 and Pd / Al 2 O 3 which use Pt or Pd alone as an oxidation catalyst, and these are effective as an oxidation catalyst for an organic solvent or CO. A single catalyst of Pd or Pd does not work effectively for oxidative removal of methane.
【０００７】このため、例えば前述希薄燃焼ガスエンジ
ンから排出される、酸素が過剰に含まれ、未燃焼ＨＣ成
分がとりわけメタンであり、また（その作動条件如何に
もよるが）通常３００〜５００℃程度で排出される排ガ
ス中のＨＣ（特に、メタン）を有効に酸化し、除去する
ためには、酸素が過剰に含まれていてもなお有効に適用
し得る酸化触媒或いは有効な処理法の開発が必要であ
る。Therefore, for example, the exhaust gas from the above-mentioned lean burn gas engine contains an excess of oxygen, the unburned HC component is especially methane, and (depending on the operating conditions thereof) usually 300 to 500 ° C. In order to effectively oxidize and remove HC (particularly methane) in exhaust gas discharged at a certain level, development of an oxidation catalyst or an effective treatment method that can be effectively applied even if oxygen is contained in excess. is necessary.
【０００８】[0008]
【発明が解決しようとする課題】本発明者は、そのよう
に希薄燃焼ガスエンジン等から排出される酸素過剰な排
ガス中のＨＣを有効に酸化し且つ耐久性のある触媒に関
し各種多方面から実験、検討を進めているうち、この触
媒としてハニカム基材にＰｔとＰｄをアルミナ担体を介
して混在させて担持させるとともに、ハニカム基材に対
する白金及びパラジウムの担持量をこれまで有効な量と
して知られていた範囲より多く、しかも特定の範囲とす
ることにより、これが有効な優れたＨＣ酸化性能を有す
るだけでなく、優れた耐久性を有し、その触媒活性を長
期にわたり安定して維持することができることを見い出
した。SUMMARY OF THE INVENTION The present inventor has conducted various experiments on a catalyst which effectively oxidizes HC in exhaust gas with excess oxygen discharged from such a lean burn gas engine and has durability. As the catalyst is being studied, Pt and Pd are mixed and supported on a honeycomb substrate through an alumina carrier as the catalyst, and the amount of platinum and palladium supported on the honeycomb substrate has been known as an effective amount so far. By setting the amount to be more than the specified range and moreover within a specific range, not only it has effective HC oxidation performance but also excellent durability, and it is possible to maintain its catalytic activity stably for a long period of time. I found what I could do.
【０００９】すなわち本発明は、酸素過剰で炭化水素を
低濃度で含む排ガス中のＨＣ酸化用として有効な触媒活
性を有し、優れた耐久性を備えたハニカム基材に担持し
た白金−パラジウム／アルミナ触媒を提供することを目
的とし、またこの触媒を使用することにより、酸素過剰
で炭化水素を低濃度で含む排ガス中のＨＣを長期にわた
り安定して酸化し、除去する方法を提供することを目的
とする。That is, according to the present invention, platinum-palladium / platinum / palladium supported on a honeycomb substrate having a catalytic activity effective for oxidizing HC in exhaust gas containing excess hydrocarbon and low concentration of hydrocarbon and having excellent durability is used. An object of the present invention is to provide an alumina catalyst, and by using this catalyst, to provide a method for stably oxidizing and removing HC in exhaust gas containing a low concentration of hydrocarbons in excess of oxygen for a long period of time. To aim.
【００１０】[0010]
【課題を解決するための手段】まず、本発明は、酸素過
剰な排ガス中の低濃度炭化水素用酸化触媒であって、ハ
ニカム基材に担持した白金−パラジウム／アルミナ触媒
からなり、該ハニカム基材に対しアルミナ担体を介して
白金とパラジウムとが混在するように担持させてなると
ともに、そのパラジウム担持量が７ｇ／ｌ以上で且つ白
金担持量が３〜２０ｇ／ｌの範囲であることを特徴とす
る酸素過剰な排ガス中の低濃度炭化水素用酸化触媒を提
供するものである。First, the present invention relates to an oxidation catalyst for low-concentration hydrocarbons in exhaust gas with excess oxygen, which comprises a platinum-palladium / alumina catalyst supported on a honeycomb substrate. The material is supported so that platinum and palladium are mixed together through an alumina carrier, and the amount of palladium supported is 7 g / l or more and the amount of platinum supported is in the range of 3 to 20 g / l. The present invention provides an oxidation catalyst for low-concentration hydrocarbons in exhaust gas containing excess oxygen.
【００１１】また、本発明は、酸素過剰で炭化水素を低
濃度で含む排ガスを、ハニカム基材に担持した白金−パ
ラジウム／アルミナ触媒からなり、該ハニカム基材に対
しアルミナ担体を介して白金とパラジウムとが混在する
ように担持させてなるとともに、そのパラジウム担持量
が７ｇ／ｌ以上で且つ白金担持量が３〜２０ｇ／ｌの範
囲である触媒に通すことを特徴とする酸素過剰で低濃度
炭化水素を含む排ガス中の炭化水素の酸化除去方法を提
供する。Further, the present invention comprises a platinum-palladium / alumina catalyst in which exhaust gas containing excess oxygen and a low concentration of hydrocarbons is carried on a honeycomb substrate, and platinum is added to the honeycomb substrate via an alumina carrier. Palladium is mixed so that it is mixed, and the amount of palladium carried is 7 g / l or more, and the amount of platinum carried is passed through a catalyst in the range of 3 to 20 g / l. Provided is a method for oxidizing and removing hydrocarbons in exhaust gas containing hydrocarbons.
【００１２】ここで、ハニカム基材に対する上記白金及
びパラジウムの担持量の単位「ｇ／ｌ」は、ハニカム基
材の１ｌ（１リットル：容積）単位に対する白金又はパ
ラジウムの担持量の意味であり、また本明細書中「ハニ
カム基材に担持した白金−パラジウム／アルミナ触媒」
とは、ハニカム基材に対してアルミナ担体を介して白金
とパラジウムとが混在するように担持された触媒である
ことを意味している。また白金の担持量は、前記のとお
り好ましくは３〜２０ｇ／ｌの範囲で担持させるが、よ
り好ましくは５〜１２ｇ／ｌの範囲で担持させる。これ
によりパラジウムを７ｇ／ｌ以上混在、担持させる点等
とも相まち、優れた耐久性を付与し、例えば空間速度
（ＳＶ）４０，０００ｈ-1という厳しい条件下でも、
Ｔ.Ｈ.Ｃ除去率４０％以上、さらにはＴ.Ｈ.Ｃ除去率４
５％以上という有効なＴ.Ｈ.Ｃ除去性能を長期にわたり
保持することができる。Here, the unit "g / l" of the amount of platinum and palladium supported on the honeycomb substrate means the amount of platinum or palladium supported on 1 l (1 liter: volume) unit of the honeycomb substrate, In the present specification, "platinum-palladium / alumina catalyst supported on a honeycomb substrate"
Means that the catalyst is carried on the honeycomb substrate so that platinum and palladium are mixed together via the alumina carrier. The amount of platinum loaded is preferably in the range of 3 to 20 g / l as described above, and more preferably in the range of 5 to 12 g / l. As a result, it is compatible with the fact that 7 g / l or more of palladium is mixed and supported, and imparts excellent durability. For example, even under severe conditions such as space velocity (SV) 40,000 h -1 ,
THC removal rate of 40% or more, further THC removal rate 4
The effective THC removal performance of 5% or more can be maintained for a long time.
【００１３】この点、例えば特開平６−２６２０８８号
には、ハニカム担体上に三層のコ−ト層を設け、その第
１コ−ト層としてＰｔ、Ｐｄ及びＲｈのうちの１種又は
２種以上の貴金属を含む活性アルミナを主成分とする無
機物を使用した排ガス浄化用触媒が記載されている。し
かし、この触媒では、その第１コ−ト層の上に第２コ−
ト層として貴金属を含まない活性アルミナを主成分とす
る無機物を施し、さらにその上にＣｕやＣｏ等の金属を
イオン交換した第３コ−ト層を設けたもので、特に実施
例の記載をみても、第１コ−ト層としてＰｔとＰｄを混
在させて担持させたものはなく、唯一ＰｄとＲｈを担持
させた例（実施例７）でも、まずＰｄを担持させた後、
次いで第２コ−ト層にＲｈを担持しており、しかもそれ
らの担持量はＰｄ＝２重量％、Ｒｈ＝１重量％と非常に
少ない。In this respect, for example, in Japanese Unexamined Patent Publication No. 6-262088, three coat layers are provided on a honeycomb carrier, and as the first coat layer, one or two of Pt, Pd and Rh is used. An exhaust gas-purifying catalyst using an inorganic material whose main component is activated alumina containing one or more noble metals is described. However, in this catalyst, a second coating is formed on the first coating layer.
An inorganic material containing activated alumina containing no noble metal as a main component is applied as a coating layer, and a third coating layer formed by ion-exchange of metals such as Cu and Co is further provided on the inorganic material. Even if it sees, there is no one in which Pt and Pd are mixed and supported as the first coat layer, and even in an example in which only Pd and Rh are supported (Example 7), first, after supporting Pd,
Next, Rh is supported on the second coat layer, and the supported amounts are very small, Pd = 2% by weight and Rh = 1% by weight.
【００１４】これに対して、本発明においては、ハニカ
ム基材に対してアルミナ担体とともにＰｔとＰｄが混在
するように担持させ、しかもハニカム基材に対してパラ
ジウムが７ｇ／ｌ以上で且つ白金の担持量を３〜２０ｇ
／ｌの範囲で担持させるが、より好ましくは５〜１２ｇ
／ｌの範囲で担持させることにより、耐久性に非常に優
れ、有効なＴ.Ｈ.Ｃ除去性能を長期にわたり保持し、持
続できるという優れた効果を得ることができるものであ
る。On the other hand, in the present invention, Pt and Pd are mixed together with the alumina carrier on the honeycomb substrate, and the honeycomb substrate contains 7 g / l or more of palladium and platinum. Carrying amount 3-20g
/ G, but more preferably 5 to 12 g
By supporting in the range of 1 / l, it is possible to obtain an excellent effect that the durability is extremely excellent and the effective THC removal performance is maintained and maintained for a long period of time.
【００１５】また、本発明におけるハニカム基材の形態
としては断面がハニカム状のもの、もしくはモノリス体
として従来知られた形状のものであれば何れも使用でき
る。図７（ａ）〜（ｂ）はその一、二の例であり、これ
ら図７（ａ）〜（ｂ）はその断面を拡大して示してい
る。これらハニカム基材の材質としては特に限定はない
が、好ましくはコ−ジェライト製又は金属製（メタル
製）のものが使用される。このうちメタルハニカムは、
好ましくは鉄−アルミニウム−クロム系合金やステンレ
ス鋼等により作られるものである。Further, as the form of the honeycomb substrate in the present invention, any one can be used as long as it has a honeycomb cross section or a form conventionally known as a monolith body. 7 (a) and 7 (b) are the first and second examples, and these FIGS. 7 (a) and 7 (b) show enlarged cross sections thereof. The material of these honeycomb substrates is not particularly limited, but cordierite or metal (metal) materials are preferably used. Of these, the metal honeycomb is
It is preferably made of an iron-aluminum-chromium alloy, stainless steel, or the like.
【００１６】次に、本発明に係るハニカム基材に担持し
た白金−パラジウム／アルミナ触媒の調製法としては、
例えばコ−ジェライト製又は金属製のハニカムをアルミ
ナの水性懸濁液でウォッシュ・コ−トし、これに白金と
パラジウムを同時に混在させ担持させて調製することが
できる。この場合その白金及びパラジウムの原料として
は、それらの塩化物、塩化アンモニウム塩、硝酸塩、酢
酸塩、ジニトロジアンミン塩、アルコキシドなどの形で
使用できる。これらの担持は、それら原料化合物を水溶
液又は水性懸濁液として含浸法やイオン交換法等を適用
し、その後常法に従って乾燥、焼成をし、金属として担
持させるものである。Next, as a method for preparing the platinum-palladium / alumina catalyst supported on the honeycomb substrate of the present invention,
For example, a honeycomb made of cordierite or a metal can be wash-coated with an aqueous suspension of alumina, and platinum and palladium can be simultaneously mixed and supported on the wash-coating. In this case, the platinum and palladium raw materials can be used in the form of their chlorides, ammonium chlorides, nitrates, acetates, dinitrodiammine salts, alkoxides and the like. For supporting these, the raw material compounds are applied as an aqueous solution or an aqueous suspension by an impregnation method, an ion exchange method or the like, and then dried and fired according to a conventional method to be supported as a metal.
【００１７】その調製法の別の態様としては、上記アル
ミナの水性懸濁液に上記白金及びパラジウムの原料化合
物をそのまま又は必要に応じて水溶液又は水性懸濁液と
して加えた後、アルミナ及びこの両原料化合物を含む水
性懸濁液によりハニカム担体をウォッシュ・コ−トし、
次いで常法に従い乾燥させ、焼成することによって作製
することもできる。また以上何れの調製態様の場合で
も、その焼成に代えて液相還元、水素還元等も適用する
ことができる。In another embodiment of the preparation method, the above-mentioned platinum and palladium raw material compounds are added to the above-mentioned aqueous suspension of alumina as it is or, if necessary, as an aqueous solution or an aqueous suspension, and then the alumina and both of them are added. Wash coating the honeycomb carrier with an aqueous suspension containing the raw material compound,
Then, it can also be produced by drying and firing according to a conventional method. Further, in any of the above-described preparation modes, liquid phase reduction, hydrogen reduction and the like can be applied instead of the firing.
【００１８】また、「酸素過剰で炭化水素（ＨＣ）を低
濃度で含む排ガス」を前述本発明に係るＨＣ酸化触媒に
より処理してＨＣを酸化除去するに際しては発熱を伴う
が、本発明によればこの熱を回収し、有効に利用するこ
とができる。このことにより「酸素過剰で炭化水素（Ｈ
Ｃ）を低濃度で含む排ガス」が前述コ−ジェネレ−ショ
ンシステムにおける希薄燃焼ガスエンジンからの排ガス
である場合にも有効に適用することができるものであ
る。Further, when "exhaust gas containing hydrocarbon (HC) at a low concentration due to excess oxygen" is treated with the HC oxidation catalyst according to the present invention to oxidize and remove HC, heat is generated, but according to the present invention. This heat can be recovered and used effectively. As a result, "hydrogen (H
It can also be effectively applied to the case where the "exhaust gas containing C) in a low concentration" is the exhaust gas from the lean-burn gas engine in the above-mentioned cogeneration system.
【００１９】図８は、本発明に係る触媒を使用する、そ
のシステムフロ−例を模式的に示した図であり、図中Ａ
は、排ガス発生源の一例として希薄燃焼ガスエンジンを
示している。例えば都市ガスを燃料として希薄燃焼ガス
エンジンＡを作動させると、ここで生成した排ガスは、
導管Ｂから（燃焼条件等の如何にもよるが）３００〜５
００℃程度で排出される。またＣは触媒容器（反応
管）、Ｄは酸化触媒層であり、この酸化触媒層Ｄとして
本発明に係るハニカム基材に担持した白金−パラジウム
／アルミナ触媒が充填、セットされる。導管Ｂからの排
ガスは、その中の微量ＨＣがここで酸化された後、導出
部Ｅから排出されるが、この処理済み排ガスはさらに必
要に応じて次の熱回収工程等へ送られる。FIG. 8 is a diagram schematically showing an example of the system flow using the catalyst according to the present invention.
Shows a lean burn gas engine as an example of an exhaust gas source. For example, when the lean burn gas engine A is operated using city gas as fuel, the exhaust gas generated here is
From conduit B (depending on combustion conditions etc.) 300-5
It is discharged at about 00 ° C. Further, C is a catalyst container (reaction tube), D is an oxidation catalyst layer, and the platinum-palladium / alumina catalyst supported on the honeycomb substrate according to the present invention is filled and set as the oxidation catalyst layer D. The exhaust gas from the conduit B is discharged from the outlet E after the trace amount of HC therein is oxidized here, and the treated exhaust gas is further sent to the next heat recovery step or the like as necessary.
【００２０】[0020]
【実施例】以下、本発明の実施例を説明するが、本発明
がこの実施例に限定されるものでないことは勿論であ
る。本実施例では、図７（ａ）で示す形態をしたハニカ
ム基材を用いた供試触媒を下記のとおりに調製し、各供
試触媒に対する性能試験を図６に示すような装置にセッ
トして実施した。EXAMPLES Examples of the present invention will be described below, but it goes without saying that the present invention is not limited to these examples. In this example, test catalysts using a honeycomb substrate having the form shown in FIG. 7A were prepared as follows, and the performance test for each test catalyst was set in an apparatus as shown in FIG. It was carried out.
【００２１】《供試触媒の調製》 （１）まず、一辺１５０ｍｍの正方形で、長さ５０ｍｍ
の直方体の、アルミナ被膜を有するコ−ジェライト製ハ
ニカム基材を準備した。（２）一方、各種濃度のジニト
ロジアミン白金及び硝酸パラジウムの酸性水性懸濁液を
作成した。これら水溶液は、ジニトロジアミン白金、硝
酸パラジウムの濃度を変え、両金属のハニカム基材への
担持量が後述の各割合となるように調製したものであ
る。（３）次いで、上記（１）のアルミナ被膜を有する
コ−ジェライト製ハニカム基材を上記（２）の水性懸濁
液中に十分に含浸させた後、エア−ガンにより過剰のス
ラリ−を除去し、温度１１５℃に１時間保持して乾燥さ
せた。<< Preparation of Test Catalyst >> (1) First, a square having a side of 150 mm and a length of 50 mm
A rectangular parallelepiped honeycomb substrate made of cordierite having an alumina coating was prepared. (2) On the other hand, an acidic aqueous suspension of various concentrations of dinitrodiamine platinum and palladium nitrate was prepared. These aqueous solutions were prepared by changing the concentrations of dinitrodiamine platinum and palladium nitrate so that the amounts of both metals supported on the honeycomb substrate would be the respective ratios described below. (3) Then, the cordierite honeycomb substrate having the alumina coating of the above (1) is sufficiently impregnated in the aqueous suspension of the above (2), and then excess slurry is removed by an air gun. Then, the temperature was kept at 115 ° C. for 1 hour to be dried.
【００２２】（４）さらに、上記乾燥物を温度５００℃
で２時間焼成し、コ−ジェライト製ハニカムに担持した
白金−パラジウム／アルミナ触媒を得た。この場合、そ
の水性懸濁液として、各々上記（２）で調製して得たジ
ニトロジアミン白金及び硝酸パラジウムを各種濃度で含
むものを使用することにより、ハニカム基材への白金と
パラジウムとの担持量が異なる白金−パラジウム／アル
ミナ触媒を調製した。また白金、パラジウムのうちの一
方のみを所定割合担持させた触媒についても同様に調製
し、これら各調製触媒を２０ｍｍφの筒状ドリルにて切
り出して１５．７ｃｃの体積の試料とし、これらを本試
験に用いる各供試触媒とした。(4) Further, the dried product is heated to a temperature of 500 ° C.
It was calcined for 2 hours to obtain a platinum-palladium / alumina catalyst supported on a cordierite honeycomb. In this case, by using as the aqueous suspension thereof, those containing dinitrodiamine platinum and palladium nitrate prepared in (2) above at various concentrations, to support platinum and palladium on the honeycomb substrate. Platinum-palladium / alumina catalysts with different amounts were prepared. Similarly, a catalyst in which only one of platinum and palladium was supported in a predetermined ratio was prepared in the same manner, and each prepared catalyst was cut out with a cylindrical drill of 20 mmφ to obtain a sample having a volume of 15.7 cc. It was used as each test catalyst used for.
【００２３】《性能試験》以上で得た各供試触媒を内径
２０ｍｍのステンレス製触媒容器（図６で云えばＣ、そ
の中に酸化触媒層Ｄとして）充填、セットし、各供試触
媒毎に以下の各条件でＨＣの酸化除去性能を調べた。試
験用の排ガスとしては、出力１５ＫＷのガスエンジンを
作動させ、ここから排出される排ガスを使用した。この
実排ガスの組成はＯ2：４．７〜５．１％、ＣＯ2：８．
９〜９．１％、水蒸気：約１０％、Ｔ.Ｈ.Ｃ（全炭化水
素）：２７００〜３２００ｐｐｍ、ＣＯ：１０００〜１
３００ｐｐｍ、ＮＯｘ：５００〜９００ｐｐｍ、Ｎ2 ：
残部（バランス）の範囲で変動しており、上記Ｔ.Ｈ.
Ｃ：２７００〜３２００ｐｐｍ中にはＣＨ4 が約８４％
含まれている。<< Performance Test >> Each of the test catalysts obtained above was filled and set in a stainless steel catalyst container (C in FIG. 6, which is an oxidation catalyst layer D therein) having an inner diameter of 20 mm, and set for each test catalyst. The oxidation removal performance of HC was examined under the following conditions. As the exhaust gas for the test, the exhaust gas discharged from the gas engine with an output of 15 kW was operated. The composition of this actual exhaust gas is O 2 : 4.7 to 5.1%, CO 2 : 8.
9 to 9.1%, steam: about 10%, THC (total hydrocarbon): 2700 to 3200 ppm, CO: 1000 to 1
300 ppm, NOx: 500 to 900 ppm, N 2 :
It fluctuates within the balance (balance) range, and the TH
C: During 2700~3200ppm CH 4 is approximately 84%
include.
【００２４】まず表１は、Ｐｄ及びＰｔのうち一方のみ
を担持させ、その量的割合を変えた場合、また両方を担
持させるが、担持量を変えた場合についてのＴ.Ｈ.Ｃ除
去率（％）への影響を試験したものである。ここで
「Ｔ.Ｈ.Ｃ除去率（％）」とは、各測定時点での触媒層
Ｄの入口部における排ガス中のＴ.Ｈ.Ｃ濃度をＸ、触媒
層Ｄの出口部におけるＴ.Ｈ.Ｃ濃度をＹとし、次式
（１）により算出したものであり、この点以下の酸化性
能試験についても同じである。First, Table 1 shows the removal rate of THC when only one of Pd and Pt is loaded and the quantitative ratio is changed, and when both are loaded, the loading amount is changed. (%) Was tested. Here, "THC removal rate (%)" means the THC concentration in the exhaust gas at the inlet of the catalyst layer D at each measurement time point X, and the T.C. at the outlet portion of the catalyst layer D. It is calculated by the following equation (1) with the HC concentration as Y, and the same applies to the oxidation performance test below this point.
【００２５】[0025]
【数 １】 [Equation 1]
【００２６】[0026]
【表 １】 [Table 1]
【００２７】表１中、はＰｄ単独を５０ｇ／ｌ、は
Ｐｄ単独を１０ｇ／ｌ担持させたものである。２０ｈ
（時間）後の時点では両者共にかなりのＴ.Ｈ.Ｃ除去活
性を示しているが、４００ｈ経過時では何れも２１％前
後のＴ.Ｈ.Ｃ除去率を示すに過ぎない。またＰｄ単独の
担持量として、ではに比べて５倍量担持させている
が、２０ｈ後のＴ.Ｈ.Ｃ除去率はでは４７．６％であ
るのに対して、では６０．３％のＴ.Ｈ.Ｃ除去率を示
し、Ｐｄ単独担持の場合、初期活性が必ずしもＰｄ担持
量の多寡に比例するのではないことを示している。In Table 1, Pd alone is loaded at 50 g / l, and Pd alone is loaded at 10 g / l. 20h
At the time point after (hours), both showed a considerable THC removal activity, but after 400 hours, all showed only a THC removal rate of about 21%. Moreover, the amount of Pd carried by itself was 5 times that of, but the THC removal rate after 20 h was 47.6%, whereas it was 60.3%. The THC removal rate is shown, showing that the initial activity is not necessarily proportional to the amount of Pd supported when Pd is supported alone.
【００２８】また〜のとおり、Ｐｔ単独を担持させ
た場合にもＴ.Ｈ.Ｃ除去率はせいぜい３４．５％（２０
ｈ後）程度で低く、またＰｔ及びＰｄの両者を担持させ
た場合にも、（このは従来の三元触媒に相当する）
や10（表中○付き10）、また〜のようにそれら両者
の担持量が共に少ないか又は一方が少ないと耐久性に劣
り、Ｔ.Ｈ.Ｃ除去活性を維持できないことを示してい
る。これに対して、、11（表中○付き11）〜12（表中
○付き12）のようにＰｔ及びＰｄの両者を従来使用され
ている量より多く担持させた場合には、４００ｈ後の時
点でも有効な優れたＴ.Ｈ.Ｃ除去活性を保持している。Further, as shown in the following, even when Pt alone is supported, the THC removal rate is at most 34.5% (20%).
After about h), it is low, and when both Pt and Pd are supported (this corresponds to a conventional three-way catalyst).
And 10 (marked with ◯ in the table), and when both of them are small as shown in (1) or (2), the durability is poor and the THC removal activity cannot be maintained. In contrast, when both Pt and Pd were loaded in amounts larger than those conventionally used, such as 11 (○ in the table 11) and 12 (○ in the table 12), after 400 h, It retains an excellent THC removal activity that is effective even at this time.
【００２９】次に、図１（ａ）〜（ｂ）は、前記調製に
より得たハニカム基材に担持した白金−パラジウム／ア
ルミナ触媒における白金−パラジウムの量的割合如何に
よるＴ.Ｈ.Ｃ除去率を調べたものである。このうち図１
（ａ）は、Ｐｔ担持量１０ｇ／ｌに対してＰｄ担持量を
変化させ、また図１（ｂ）は、Ｐｄ担持量１０ｇ／ｌに
対して、Ｐｔ担持量を変化させた各供試触媒を使用して
実施した結果である。操作条件は、反応温度６５８Ｋ
（３８５℃）、空間速度ＳＶ＝４０，０００ｈ-1とし、
反応開始後４００時間経過した時点での測定結果を示し
ている。Next, FIGS. 1 (a) and 1 (b) show the removal of THC according to the quantitative ratio of platinum-palladium in the platinum-palladium / alumina catalyst supported on the honeycomb substrate obtained by the above preparation. It is a survey of rates. Of these, Figure 1
(A) shows the Pd loading amount varied with respect to the Pt loading amount of 10 g / l, and FIG. 1 (b) shows each Pt loading amount varied with respect to the Pd loading amount of 10 g / l. It is the result of carrying out using. Operating conditions are reaction temperature 658K
(385 ° C.), space velocity SV = 40,000 h −1 ,
The measurement results at the time when 400 hours have elapsed after the start of the reaction are shown.
【００３０】図１（ａ）のとおり、まず担持Ｐｄ量がゼ
ロ、すなわちＰｔだけを１０ｇ／ｌ担持させた場合に
は、Ｔ.Ｈ.Ｃ除去率は２５％程度を示すに過ぎないが、
以降担持Ｐｄ量を漸次増加させて行くに従い、Ｔ.Ｈ.Ｃ
除去率は急激に増大して行くことが分かる。また図１
（ｂ）のとおり、Ｐｄ担持量１０ｇ／ｌで、担持Ｐｔ量
がゼロすなわちＰｄだけを担持させた場合、Ｔ.Ｈ.Ｃ除
去率は１７％程度を示すに過ぎない。しかし担持Ｐｔ量
をゼロから漸次増加させて行くと、Ｔ.Ｈ.Ｃ除去率は急
激に増大して行き、担持Ｐｔ量約７．５ｇ／ｌでピ−ク
（Ｔ.Ｈ.Ｃ除去率５０％強）となる。以降除去率は徐々
に低下して行くが、担持Ｐｔ量１５ｇ／ｌで４２％強、
担持Ｐｔ量２０ｇ／ｌでもなお約４０％の除去率を示し
ている。As shown in FIG. 1A, when the amount of supported Pd is zero, that is, when only Pt is supported at 10 g / l, the THC removal rate shows only about 25%.
After that, as the supported Pd amount was gradually increased, THC
It can be seen that the removal rate increases rapidly. See also FIG.
As shown in (b), when the Pd supported amount is 10 g / l and the supported Pt amount is zero, that is, when only Pd is supported, the THC removal rate shows only about 17%. However, when the supported Pt amount was gradually increased from zero, the THC removal rate rapidly increased, and the peak (THC removal rate was increased at a supported Pt amount of about 7.5 g / l. 50%). After that, the removal rate gradually decreases, but when the supported Pt amount is 15 g / l, it is more than 42%,
Even when the amount of supported Pt was 20 g / l, the removal rate was still about 40%.
【００３１】さらに図２は、酸化触媒として担持Ｐｔ量
を１０ｇ／ｌ、担持Ｐｄ量を１０ｇ／ｌ混在、担持させ
た供試触媒を用いて実施した耐久試験の結果である。こ
こでの操作条件は、反応温度６７３Ｋ（４００℃）、空
間速度（ＳＶ）は実験開始時から最初の５５０時間は４
０，０００ｈ-1とし、それ以降１４００時間経過時まで
２０，０００ｈ-1に下げた後、再び４０，０００ｈ-1に
戻して実施した。Further, FIG. 2 shows the results of a durability test carried out by using a test catalyst which was loaded with a supported Pt amount of 10 g / l and a supported Pd amount of 10 g / l as an oxidation catalyst. The operating conditions here are a reaction temperature of 673 K (400 ° C.) and a space velocity (SV) of 4 for the first 550 hours from the start of the experiment.
It was set to 50,000 h −1, and after that, it was lowered to 20,000 h −1 until 1400 hours passed, and then it was returned to 40,000 h −1 again.
【００３２】図２のとおり、本発明に係る酸化触媒は１
９００時間（８０日）強にも及ぶ連続使用後でもその触
媒性能に殆んど変化がなく、優れた耐久性を備えている
ことが分かる。すなわちＴ.Ｈ.Ｃ除去率は、実験開始当
初の８０％強から１００時間経過時まで幾分低下はする
が、その後５８％前後のＴ.Ｈ.Ｃ除去率を維持してい
る。途中空間速度（ＳＶ）を２０，０００ｈ-1に下げる
と６３％前後に上昇し、以降４０，０００ｈ-1に上げる
時点までこの除去率を維持し、再び４０，０００ｈ-1に
戻してもその酸化性能上の変化は殆んどみられない。As shown in FIG. 2, the oxidation catalyst according to the present invention is 1
It can be seen that even after continuous use for more than 900 hours (80 days), the catalyst performance hardly changed and the catalyst had excellent durability. That is, the THC removal rate slightly decreases from a little over 80% at the beginning of the experiment to 100 hours later, but after that, the THC removal rate of around 58% is maintained. The middle space velocity (SV) raised to 63% before and after lowering the 20,000 h -1, and maintaining the removal rate to the point where increased after 40,000h -1, be returned back to 40,000H -1 Almost no change in oxidation performance was observed.
【００３３】また、図３は、図１（ａ）に示したＰｄの
担持割合のうちから３点をとり、Ｐｔ量に対するＰｄ量
の影響を経時的に試験した結果である。すなわち、ハニ
カム担体に対する担持量として、Ｐｔ量を１０ｇ／ｌで
一定とし、Ｐｄ量をそれぞれ１．０ｇ／ｌ、５．０ｇ／
ｌ及び１０ｇ／ｌとした各供試触媒によるＴ.Ｈ.Ｃ除去
率を示している。ここでの操作条件は、図１（ａ）の場
合と同じく、反応温度を６５８Ｋ（３８５℃）、空間速
度（ＳＶ）は４０，０００ｈ-1とし、また試験時間は５
００時間継続させた。Further, FIG. 3 shows the results of time-course tests of the influence of the Pd amount on the Pt amount by taking three points from the Pd loading ratio shown in FIG. 1 (a). That is, as the loading amount on the honeycomb carrier, the Pt amount was kept constant at 10 g / l, and the Pd amounts were 1.0 g / l and 5.0 g / l, respectively.
The THC removal rates of the respective tested catalysts of 1 and 10 g / l are shown. The operating conditions here are the same as in the case of FIG. 1A, the reaction temperature was 658 K (385 ° C.), the space velocity (SV) was 40,000 h −1 , and the test time was 5
It was continued for 00 hours.
【００３４】図３のとおり、Ｐｔ量１０ｇ／ｌに対して
Ｐｄ量を１．０ｇ／ｌとした供試触媒では当初からＴ.
Ｈ.Ｃ除去率３０％前後を示すに過ぎない。また同じく
Ｐｄ量を５．０ｇ／ｌとしたものでは、当初は５０％を
超える値を示すが、５０時間経過後には４０％を切り、
以降３７〜３８％を示すに過ぎない。一方、担持Ｐｔ量
１０ｇ／ｌに対し担持Ｐｄ量を１０．０ｇ／ｌとしたも
のでは、５００時間経過時点でも４７〜４８％のＴ.Ｈ.
Ｃ除去率を維持している。As shown in FIG. 3, the test catalyst having a Pd content of 10 g / l and a Pd content of 1.0 g / l had T.S.
The HC removal rate is only about 30%. Similarly, when the amount of Pd is 5.0 g / l, the value initially exceeds 50%, but after 50 hours has passed below 40%,
After that, it shows only 37 to 38%. On the other hand, when the supported Pd amount was 10.0 g / l with respect to the supported Pt amount of 10 g / l, the T.H.
The C removal rate is maintained.
【００３５】また図４は、担持Ｐｔ量に対するＰｄ担持
量の影響を経時的変化とともに試験した結果である。こ
こでは図１（ｂ）における５点、すなわち担持Ｐｄ量を
１０ｇ／ｌとし、担持Ｐｔ量を０．１ｇ／ｌ、１．０ｇ
／ｌ、５．０ｇ／ｌ、８．０ｇ／ｌ及び１０ｇ／ｌとし
た各供試触媒によるＴ.Ｈ.Ｃ除去率を示している。操作
条件は、図２（ｂ）の場合と同じく、反応温度を６５８
Ｋ（３８５℃）、空間速度（ＳＶ）は４０，０００ｈ-1
とし、また試験時間は５００時間である。FIG. 4 shows the results of testing the influence of the amount of Pd supported on the amount of Pt supported, along with changes over time. Here, the five points in FIG. 1B, that is, the amount of supported Pd is 10 g / l, and the amount of supported Pt is 0.1 g / l and 1.0 g.
2 shows the THC removal rates of the respective tested catalysts of 1 / l, 5.0 g / l, 8.0 g / l and 10 g / l. The operating condition is that the reaction temperature is 658 as in the case of FIG.
K (385 ° C), space velocity (SV) 40,000 h -1
And the test time is 500 hours.
【００３６】図４のとおり、Ｐｄ量１０ｇ／ｌに対し
て、Ｐｔ量を０．１ｇ／ｌとしたものでは５０時間経過
後、Ｔ.Ｈ.Ｃ除去率２０％弱を示すに過ぎず、この点Ｐ
ｔ量を１．０ｇ／ｌとしたものでも３０％前後を示して
いるに過ぎない。またＰｔ量を５．０ｇ／ｌとしたもの
では、試験当初は５０％を超える値を示すが、５０時間
経過後には４０％を切り、以降３７〜３８％程度の除去
率で推移しているに過ぎない。これに対して、担持Ｐｔ
量を１０．０ｇ／ｌとしたものでは５００時間経過時点
でも４７〜４８％のＴ.Ｈ.Ｃ除去率を維持しおり、この
点Ｐｔ量を８．０ｇ／ｌとした供試触媒ではさらに高い
酸化性能を示している。As shown in FIG. 4, when the amount of Pt was 0.1 g / l with respect to the amount of Pd of 10 g / l, after 50 hours, the THC removal rate showed only 20% or less. This point P
Even when the t amount is set to 1.0 g / l, it shows only about 30%. Further, when the amount of Pt is 5.0 g / l, the value exceeds 50% at the beginning of the test, but it is below 40% after 50 hours, and thereafter, the removal rate is about 37 to 38%. Nothing more than. On the other hand, supported Pt
When the amount was 10.0 g / l, the THC removal rate of 47 to 48% was maintained even after 500 hours, and this point was higher in the test catalyst with Pt amount of 8.0 g / l. It shows the oxidation performance.
【００３７】《アルミナ担体層に対するＰｄ及びＰｔの
存在状態如何による効果》以上の諸例は、ＰｄとＰｔと
を一層のアルミナ担体層に混在するように担持させた触
媒を用いた例であるが、以下はＰｄとＰｔとを一層のア
ルミナ担体層に混在するよう担持させた場合（実施例）
とＰｄとＰｔとを別々のアルミナ担体層に担持させた場
合（比較例）との触媒性能、耐久性如何を試験したもの
である。<< Effect of Pd and Pt Presence on Alumina Carrier Layer >> The above examples are examples using a catalyst in which Pd and Pt are mixed so as to be mixed in one alumina carrier layer. The following is a case where Pd and Pt are mixed and supported in a single alumina carrier layer (Example)
And Pd and Pt supported on different alumina carrier layers (comparative example) were tested for catalyst performance and durability.
【００３８】ここでの実施例用触媒としては、表１中試
験番号の場合と同様にしてパラジウム及び白金の各１
０ｇ／ｌを単一のアルミナ担体層に混在するように担持
させたものを使用し、一方比較例用触媒は、次のように
調製した。前記アルミナ被膜を有するコ−ジェライト製
ハニカム基材に硝酸パラジウム水溶液によりパラジウム
を１０ｇ／ｌ担持させた後、その上に再びアルミナ担体
をその懸濁液としてウォッシュコ−ト法でコ−トし、こ
れに対してジニトロジアミン白金水溶液を用いて１０ｇ
／ｌ白金を担持させた。この場合乾燥や焼成処理、筒状
ドリルによる切り出し等は前記と同様に行った。As the catalysts for the examples here, one each of palladium and platinum was used as in the case of the test number in Table 1.
A catalyst prepared by mixing 0 g / l so as to be mixed in a single alumina carrier layer was used, while a catalyst for a comparative example was prepared as follows. After 10 g / l of palladium was supported on the cordierite honeycomb substrate having the alumina coating by an aqueous solution of palladium nitrate, the alumina carrier was again coated on the honeycomb substrate as a suspension thereof by the wash coat method, On the other hand, 10 g using a dinitrodiamine platinum aqueous solution
/ L platinum was supported. In this case, drying, firing, cutting with a cylindrical drill, etc. were performed in the same manner as above.
【００３９】図５は、それら両触媒を用いて前述と同様
にして実施した耐久試験の結果を示すものである。図５
のとおり、実施例触媒では、５０ｈ経過時点で６２％程
度のＴ.Ｈ.Ｃ除去率を示し、１５０ｈ経過時以降でも４
７％前後のＴ.Ｈ.Ｃ除去率を保持している。これに対し
て、比較例触媒では、当初の５４％から徐々に低下して
行き、５００ｈ経過時点では２８％程度のＴ.Ｈ.Ｃ除去
率となってしまっている。このように有効な耐久性を得
る上では、Ｐｄ及びＰｔを単一のアルミナ担体層に混在
するように担持させる必要があることが明らかである。FIG. 5 shows the results of a durability test carried out in the same manner as above using both of these catalysts. Figure 5
As shown in the above, the Example catalysts showed a THC removal rate of about 62% after 50 hours, and 4 hours even after 150 hours.
It has a THC removal rate of around 7%. On the other hand, in the catalyst of Comparative Example, it gradually decreased from the initial 54%, and after 500 hours, the THC removal rate was about 28%. It is clear that it is necessary to support Pd and Pt so that they are mixed in a single alumina carrier layer in order to obtain effective durability.
【００４０】さらに図６（ａ）〜（ｂ）は、ＥＰＭＡ
（Ｘ線マイクロアナライザ−、Electron Probe Micro-a
nalyser） 分析により、上記実施例触媒及び比較例触媒
中におけるＰｔ、Ｐｄの存在状態を調べたものである。
図６（ａ）のとおり、実施例触媒では、コ−ジェライト
基材上のアルミナ層中に均一に混在していることが分か
る。一方、図６（ｂ）に示す比較例触媒については、二
層のアルミナ層のそれぞれにＰｔ及びＰｄが別個に担持
されている（なお、比較例触媒では、第１アルミナ層す
なわちコ−ジェライト基材上のアルミナ層中にもＰｔの
スペクトルが現れているが、これはＰｔを第２アルミナ
層へ担持させるに際してＰｔが第１層まで浸透したもの
と解される）。Further, FIGS. 6A and 6B show EPMA.
(X-ray micro analyzer, Electron Probe Micro-a
nalyser) The presence state of Pt and Pd in the catalyst of the above-mentioned example and the catalyst of the comparative example were examined by analysis.
As shown in FIG. 6 (a), it can be seen that the catalysts of Examples are uniformly mixed in the alumina layer on the cordierite substrate. On the other hand, in the comparative example catalyst shown in FIG. 6 (b), Pt and Pd are separately supported on each of the two alumina layers (in the comparative example catalyst, the first alumina layer, that is, the cordierite group). A spectrum of Pt also appears in the alumina layer on the material, which is understood to be that Pt has penetrated to the first layer when Pt is supported on the second alumina layer).
【００４１】[0041]
【発明の効果】以上のとおり、本発明に係る炭化水素酸
化触媒は、酸素過剰な排ガス中の低濃度炭化水素に対す
る有効な酸化性能を長期にわたり維持することができ
る。またその酸化により発熱を伴うことから、熱回収が
可能であり、このため特に都市ガス等を駆動源とするコ
−ジェネレ−ションシステムにおける希薄燃焼ガスエン
ジンからの排ガスに対しても有効に適用できる。さらに
本発明に係る炭化水素酸化触媒は、優れた耐久性を有す
ることから、交換頻度を格段に少なくでき、排ガス処理
システムの低コスト化を図ることができる。INDUSTRIAL APPLICABILITY As described above, the hydrocarbon oxidation catalyst according to the present invention can maintain an effective oxidation performance for low concentration hydrocarbons in exhaust gas with excess oxygen for a long period of time. In addition, since heat is generated due to the oxidation, heat can be recovered. Therefore, it can be effectively applied to exhaust gas from a lean-burn gas engine particularly in a co-generation system using city gas as a driving source. . Furthermore, since the hydrocarbon oxidation catalyst according to the present invention has excellent durability, the replacement frequency can be significantly reduced, and the cost of the exhaust gas treatment system can be reduced.
【図面の簡単な説明】[Brief description of drawings]
【図１】ハニカム基材に担持した白金−パラジウム／ア
ルミナ触媒における白金−パラジウムの量的割合如何に
よるＴ.Ｈ.Ｃ除去率を示す図。FIG. 1 is a diagram showing the THC removal rate depending on the quantitative ratio of platinum-palladium in a platinum-palladium / alumina catalyst supported on a honeycomb substrate.
【図２】供試触媒として担持Ｐｔ量が１０ｇ／ｌ、担持
Ｐｄ量が１０ｇ／ｌの供試触媒を用いて実施した耐久試
験の結果を示す図。FIG. 2 is a diagram showing a result of a durability test carried out using a test catalyst having a supported Pt amount of 10 g / l and a supported Pd amount of 10 g / l as a test catalyst.
【図３】Ｐｔ量に対するＰｄ量の影響を経時的に試験し
た結果を示す図。FIG. 3 is a diagram showing a result of time-dependent testing of the influence of Pd amount on Pt amount.
【図４】Ｐｄ量に対するＰｔ量の影響を経時的に試験し
た結果を示す図。FIG. 4 is a diagram showing the results of a test of the influence of the amount of Pt on the amount of Pd over time.
【図５】触媒中のＰｄとＰｔの存在状態如何による耐久
性試験結果を示す図。FIG. 5 is a view showing a result of a durability test depending on the presence state of Pd and Pt in a catalyst.
【図６】実施例触媒と比較例触媒に対するＥＰＭＡ分析
結果を示す図。FIG. 6 is a diagram showing EPMA analysis results for the example catalyst and the comparative example catalyst.
【図７】本発明で使用するハニカム基材の例を示す図
（断面模式図）。FIG. 7 is a view (cross-sectional schematic view) showing an example of a honeycomb substrate used in the present invention.
【図８】本発明触媒を使用するシステムフロ−例の模式
図。FIG. 8 is a schematic diagram of an example of a system flow using the catalyst of the present invention.
Ａ 希薄燃焼ガスエンジン Ｂ 導管 Ｃ 触媒容器（反応管） Ｄ 酸化触媒層 Ｅ 導出管 A lean-burn gas engine B conduit C catalyst container (reaction tube) D oxidation catalyst layer E outlet pipe
Claims (6)
化触媒であって、ハニカム基材に担持した白金−パラジ
ウム／アルミナ触媒からなり、該ハニカム基材に対しア
ルミナ担体を介して白金とパラジウムとが混在するよう
に担持させてなるとともに、そのパラジウム担持量が７
ｇ／ｌ以上で且つ白金担持量が３〜２０ｇ／ｌの範囲で
あることを特徴とする酸素過剰な排ガス中の低濃度炭化
水素用酸化触媒。1. An oxidation catalyst for low-concentration hydrocarbons in exhaust gas in excess of oxygen, comprising a platinum-palladium / alumina catalyst supported on a honeycomb substrate, and platinum on the honeycomb substrate via an alumina carrier. It is supported so that it is mixed with palladium, and the amount of palladium supported is 7
An oxidation catalyst for low-concentration hydrocarbons in exhaust gas in excess of oxygen, characterized in that the amount of platinum supported is in the range of 3 to 20 g / l or more.
る請求項１記載の酸素過剰な排ガス中の低濃度炭化水素
用酸化触媒。2. The oxidation catalyst for low-concentration hydrocarbon in exhaust gas having excess oxygen according to claim 1, wherein the main component of the low-concentration hydrocarbon is methane.
金属製である請求項１又は２記載の酸素過剰な排ガス中
の低濃度炭化水素用酸化触媒。3. The oxidation catalyst for low-concentration hydrocarbons in exhaust gas with excess oxygen according to claim 1 or 2, wherein the honeycomb substrate is made of cordierite or metal.
を、ハニカム基材に担持した白金−パラジウム／アルミ
ナ触媒からなり、該ハニカム基材に対しアルミナ担体を
介して白金とパラジウムとが混在するように担持させて
なるとともに、そのパラジウム担持量が７ｇ／ｌ以上で
且つ白金担持量が３〜２０ｇ／ｌの範囲である触媒に通
すことを特徴とする酸素過剰で低濃度炭化水素を含む排
ガス中の炭化水素の酸化除去方法。4. A platinum-palladium / alumina catalyst in which exhaust gas containing a low concentration of hydrocarbons in excess of oxygen is carried on a honeycomb substrate, and platinum and palladium are mixed on the honeycomb substrate via an alumina carrier. And a low-concentration hydrocarbon in excess oxygen, which is characterized by being passed through a catalyst having a palladium loading of 7 g / l or more and a platinum loading of 3 to 20 g / l. A method for oxidizing and removing hydrocarbons in exhaust gas.
る請求項４記載の酸素過剰で低濃度炭化水素を含む排ガ
ス中の炭化水素の酸化除去方法。5. The method for oxidizing and removing hydrocarbons in exhaust gas containing low concentration hydrocarbons in excess of oxygen according to claim 4, wherein the main component of the low concentration hydrocarbons is methane.
スが希薄燃焼ガスエンジンからの排ガスである請求項４
又は５記載の酸素過剰で低濃度炭化水素を含む排ガス中
の炭化水素の酸化除去方法。6. The exhaust gas containing excess oxygen and low concentration hydrocarbons is exhaust gas from a lean burn gas engine.
Alternatively, the method for oxidizing and removing hydrocarbons in exhaust gas containing low concentration hydrocarbons in excess of oxygen according to 5 above.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16795595A JP3270295B2 (en) | 1995-06-09 | 1995-06-09 | Oxidation catalyst for unburned hydrocarbons in exhaust gas and method for removing the same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16795595A JP3270295B2 (en) | 1995-06-09 | 1995-06-09 | Oxidation catalyst for unburned hydrocarbons in exhaust gas and method for removing the same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08332392A true JPH08332392A (en) | 1996-12-17 |
| JP3270295B2 JP3270295B2 (en) | 2002-04-02 |
Family
ID=15859149
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|---|---|---|---|
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000061308A (en) * | 1998-06-08 | 2000-02-29 | Osaka Gas Co Ltd | Catalyst and method for cleaning exhaust gas |
| JP2000342972A (en) * | 1999-06-02 | 2000-12-12 | Osaka Gas Co Ltd | Catalyst for purifying exhaust gas and exhaust gas purifying method |
| JP2002166172A (en) * | 2000-09-20 | 2002-06-11 | Toyota Motor Corp | Catalyst for cleaning exhaust gas |
| KR100435438B1 (en) * | 1999-12-23 | 2004-06-10 | 주식회사 포스코 | Palladium-platinum/titania catalyst and a method for removing hydrocarbon by using the catalyst |
| JP2007075707A (en) * | 2005-09-13 | 2007-03-29 | Hino Motors Ltd | Exhaust cleaner |
| JP2007083224A (en) * | 2005-08-23 | 2007-04-05 | Mazda Motor Corp | Diesel particulate filter |
| WO2007129430A1 (en) * | 2006-05-01 | 2007-11-15 | Ibiden Co., Ltd. | Honeycomb structure, process for producing honeycomb structure, honeycomb filter and process for producing honeycomb filter |
| US7364712B2 (en) | 2000-11-17 | 2008-04-29 | Osaka Gas Company Limited | Catalyst for purifying methane-containing waste gas and method of purifying methane-containing waste gas |
| JP4522512B2 (en) * | 1999-11-05 | 2010-08-11 | 東京瓦斯株式会社 | Low concentration hydrocarbon oxidation catalyst in exhaust gas and method for producing the same |
-
1995
- 1995-06-09 JP JP16795595A patent/JP3270295B2/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000061308A (en) * | 1998-06-08 | 2000-02-29 | Osaka Gas Co Ltd | Catalyst and method for cleaning exhaust gas |
| JP2000342972A (en) * | 1999-06-02 | 2000-12-12 | Osaka Gas Co Ltd | Catalyst for purifying exhaust gas and exhaust gas purifying method |
| JP4522512B2 (en) * | 1999-11-05 | 2010-08-11 | 東京瓦斯株式会社 | Low concentration hydrocarbon oxidation catalyst in exhaust gas and method for producing the same |
| KR100435438B1 (en) * | 1999-12-23 | 2004-06-10 | 주식회사 포스코 | Palladium-platinum/titania catalyst and a method for removing hydrocarbon by using the catalyst |
| JP2002166172A (en) * | 2000-09-20 | 2002-06-11 | Toyota Motor Corp | Catalyst for cleaning exhaust gas |
| US7364712B2 (en) | 2000-11-17 | 2008-04-29 | Osaka Gas Company Limited | Catalyst for purifying methane-containing waste gas and method of purifying methane-containing waste gas |
| JP2007083224A (en) * | 2005-08-23 | 2007-04-05 | Mazda Motor Corp | Diesel particulate filter |
| JP2007075707A (en) * | 2005-09-13 | 2007-03-29 | Hino Motors Ltd | Exhaust cleaner |
| WO2007129430A1 (en) * | 2006-05-01 | 2007-11-15 | Ibiden Co., Ltd. | Honeycomb structure, process for producing honeycomb structure, honeycomb filter and process for producing honeycomb filter |
| US7576035B2 (en) | 2006-05-01 | 2009-08-18 | Ibiden Co., Ltd. | Honeycomb structure and method for manufacturing honeycomb structure |
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