Patent Application
20080305022
The subject of the invention is a goldcatalyst, a method for its production and its use.
Gold with a large particle size has been regarded as a poorly active catalyst.
A theoretical calculation has explained the smooth surface of Au is noble in the dissociation adsorption of hydrogen (Hammer and Norskov, 1995).
However, when Au is deposited on nanoparticles like metal oxides by means of coprecipitation and deposition-precipitation techniques, it exhibits surprisingly high catalytic activity for CO oxidation at a temperature as low as 200 K (Haruta et al. 1989; Haruta and Daté, 2001). This finding has motivated many scientists and engineers to investigate in the catalysis of Au since 1990.
Many excellent reviews have been reported (Bond and Thompson, 1999; 2000; Cosandey and Madey, 2001; Kozlov et al., 1999; Haruta, 1997a, b; Haruta and Date, 2001; Okumura, 1999).
The selective removal of CO in a hydrogen rich gas under ambient conditions has been of considerable technical interest for purification of hydrogen rich gas, e.g. for H2 supply in ammonia synthesis for a long time.
In recent years, this technology has attracted new interest due to its use in fuel cell technology.
Polymer electrolyte membrane fuel cells (PEMFC), in particular in vehicle applications, operate at relatively low temperatures, usually at 80-120° C.
When hydrogen rich fuel is produced from methanol or gasoline on board by partial oxidation and steam reforming combined with water gas shift reaction, the Pt anodes at these low temperatures are often poisoned by incomplete combustion produces, mainly CO, reducing the overall fuel cell performance. Under normal running conditions, the product hydrogen stream contains approximately 75 vol. % H2, 25 vol. % CO2, a few vol. % H2O, and 0.5-1.0 vol. % CO.
Thus in order to obtain optimum performance for the fuel cell vehicles, the total concentration of CO in the gas stream should be reduced, if possible, to below 100 ppm.
Metal oxide-supported nanosized gold catalysts are very active for CO oxidation at low temperature. The suitable supports are the metal oxides which can be partially reduced, such as TiO2, Fe2O3, CO3O4, etc.
CeO2 was used as a support because of its high oxygen storage capacity. Although several ceria-supported catalysts were reported before, most of their loading metals were not gold or different methods were used to prepare the catalysts.
CeO2 has been used as the support for platinum (Holgado and Munuera, 1995), palladium (Yee et al., 1999), rhodium (Yee et al., 2000) and copper oxide (Avgouropoulos et al., 2002).
Antonucci et al. (2004) prepared the CeO2 supported gold catalysts by coprecipitation method and used it on selective CO oxidation.
Osuwan et al. (2004) also prepared the gold/cerium oxide catalysts by three methods, co-precipitation, impregnation and sol-gel, and used it on water-gas shift reaction.
Hutchings et al. (1998) investigated in detail the effect of preparation conditions on copper containing catalysts, Cu—Mn—O catalysts, on the performance of catalytic removal of CO.
Another type of catalysts proposed for selective CO oxidation were noble metals, such as platinum, ruthenium and rhodium, supported on alumina and zeolite.
The Freni et al. (2000) investigation showed that Ru/Al2O3 and Rh/Al2O3 catalysts had higher selectively and reactivity for catalytic removal by oxidation of CO compared with a Pt/Al2O3 catalyst.
Lee et al. (1998) studied the catalytic performance of removal of CO by the selective catalytic oxidation method based on Pt/Al2O3 and A-zeolite, respectively.
Kahlich et al. (1997) investigated the kinetics of selective CO oxidation on Pt/Al2O3.
Dong et al. (1997) investigated the performance of oxidation of CO over supported PdCl2—CuCl2 catalysts, and also studied the effect of small amounts of impurities, such as HCl and SO2, on the catalyst performance.
Avgouropoulos et al. (2002) compared the Pt/r-Al2O3, Au/a-Fe2O3 and CuO—CeO2 catalysts for the selective oxidation of CO in hydrogen rich gas. The Au/a-Fe2O3 catalyst is superior to the other two for the reaction at relatively low reaction temperatures (<80-120° C., depending on contact time and feed composition employed), while at higher reaction temperatures, best results are obtained with the CuO—CeO2 catalyst, which proved to be more active and remarkably more selective than the Pt/r-Al2O3 catalyst. The Au/a-Fe2O3 catalyst was the most sensitive, while the Pt/r-Al2O3 the most resistant towards deactivation caused by the presence of CO2 and H2O in the feed. In addition, the Au/a-Fe2O3 lost a considerable portion of its activity during the first 80 h under reaction condition, the CuO—CeO2 and Pt/r-Al2O3 catalysts exhibited a stable catalytic performance, at least, during the time-period of 7-8 days. In contrast, Cameron (2003) reported that Au/a-Fe2O3 is much more reactive than Pt/r-Al2O3.
Several literatures have been reported about selective CO oxidation as shown in table 3.
It is found that most gold/ceria oxide catalysts do not show very high activities below 100° C. which is better for PROX reaction.
The cited references are published in
The subject of the invention is a goldcatalyst, characterized in that the gold is supported on ceria.
In a preferred form of the invention the ceria is a polycrystalline cerium oxide powder in the form of aggregates of primary particles, which has
The ceria can be a Ce1-xMnxO2 support. The Ce1-xMnxO2 support can contain the elements in the ratio Ce:Mn=10:1 to 1:1.
The Ce1-xMnxO2 support can be prepared via the impregnation method, whereby a solution of a Mn-salt is added to the CeO2 powder and the impregnated CeO2 powder is then calcined.
The calcination can be made at a temperature of 350° C. to 450° C. for a time of up to 3 hours.
The ceria used according to the invention can be a known ceria, i.e. the ceria that is disclosed in EP 1506940A1 (=US 2005/036928A1) or that is disclosed in the German patent application DE 102005344, filed on Feb. 5, 2005.
According to DE 102005344 the ceria can be produced by a process by reacting an aerosol with oxygen in a reaction space at a reaction temperature of more than 700° C. and then separating the resulting powder from the gaseous substances, wherein
The volume-related mean drop diameter D30 is calculated by:
A starting material is to be understood as being a cerium compound which is converted under the reaction conditions into a cerium oxide.
It is possible to produce cerium oxide powders having a large surface area if the volume-related mean drop diameter D30 is from 30 to 100 μm and at the same time up to 10% of the drops are absolutely larger than 100 μm. It is possible as a result to increase the throughput of solution compared with the prior art without having to accept a marked reduction in the BET surface areas of the powders. The BET surface area of the powders obtained by the process according to the invention is at least 20 m2/g, preferably from 20 to 200 m2/g.
The absolute drop size is determined according to the principle of dual phase-Doppler anemometry using a 5 W argon-ion continuous-wave laser.
In a preferred embodiment, the number of drops, based on the total number of drops, larger than 100 μm may be from 3% to 8%.
Furthermore, it may be advantageous if the percentage of drops larger than 250 μm is not more than 10%, based on the number of drops >100 μm.
In particular, an embodiment may be advantageous in which the following dependence of the volume-related mean drop diameter D30 on the spray width of the aerosol applies:
The throughput of a solution containing a starting material may be preferably from 1.5 to 2000 kg/h and particularly preferably from 100 to 500 kg/h.
The content of starting material in the solution may be from 2 to 60 wt. %, preferably from 5 to 40 wt. %.
The starting materials may be organometallic and/or inorganic in nature; preference may be given to organometallic compounds. Examples of inorganic starting materials may be in particular cerium chlorides and cerium nitrates. There may be used as organometallic compounds especially cerium alcoholates and/or cerium carboxylates. There may be used as alcoholates preferably ethoxides, n-propoxides, isopropoxides, n-butoxides and/or tert.-butoxides. As carboxylates there may be used the compounds underlying acetic acid, propionic acid, butanoic acid, hexanoic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, octanoic acid, 2-ethylhexanoic acid, valeric acid, capric acid and/or lauric acid. 2-ethylhexanoates and/or laurates may particularly advantageously be used.
Inorganic starting compounds may preferably be dissolved in water; organometallic starting compounds may preferably be dissolved in organic solvents.
As organic solvents, or as a constituent of organic solvent mixtures, there may be used preferably alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol or tert.-butanol, diols such as ethanediol, pentanediol, 2-methyl-2,4-pentanediol, dialkyl ethers such as diethyl ether, tert.-butyl methyl ether or tetrahydrofuran, C1-C12-carboxylic acids such as, for example, acetic acid, propionic acid, butanoic acid, hexanoic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, octanoic acid, 2-ethylhexanoic acid, valeric acid, capric acid, lauric acid. There may further be used ethyl acetate, benzene, toluene, naphtha and/or benzine. Preference is given to the use of solutions containing C2-C12-carboxylic acids, in particular 2-ethylhexanoic acid and/or lauric acid.
Preferably, the content of C2-C12-carboxylic acids in the solution is less than 60 wt. %, particularly preferably less than 40 wt. %, based on the total amount of solution.
In a particularly preferred embodiment, the solutions of the starting materials contain at the same time a carboxylate and the underlying carboxylic acid and/or an alcoholate and the underlying alcohol. In particular, there may be used as starting materials 2-ethylhexanoates in a solvent mixture that contains 2-ethylhexanoic acid.
There may be used as a reactive gas such as air, air enriched with oxygen and/or an inert gas such as nitrogen. In general, air is used as the atomising gas.
With regard to the amount of atomising gas, the ratio throughput of the solution of the starting material/amount of atomising gas is preferably from 2 to 25 kg/Nm3 and particularly preferably from 5 to 10 kg/Nm3.
Suitable multi-component nozzles are especially three-component nozzles or four-component nozzles.
When three-component nozzles or four-component nozzles are used it is possible to atomise, in addition to the atomising gas, two, or three, separate solutions which contain
It is thus possible, for example, simultaneously to atomise two solutions having different concentrations of a starting material with the same solvent or solvent mixture. Aerosol drops of different sizes are thereby obtained.
It is also possible, for example, for the atomising gas to be supplied via two nozzles or for different atomising gases to be used, for example air and steam.
Separate solutions of different starting materials can be used to produce mixed oxide powders.
The reaction temperature of more than 700° C. can preferably be obtained by means of a flame produced by reaction of a hydrogen-containing combustion gas with (primary) air, optionally enriched with oxygen. Suitable combustion gases may be hydrogen, methane, ethane, propane, butane and/or natural gas, with hydrogen being particularly preferred. The reaction temperature is defined as the temperature that is established 0.5 m below the flame.
It may further be advantageous if secondary air is additionally introduced into the reaction space. In general, the amount of secondary air will be such that the ratio of secondary air to primary air is from 0.1 to 10.
It is particularly advantageous if lambda is ≧1.5, lambda being calculated from the quotient of the sum of the oxygen content in the air used (primary air, secondary air and atomising air) divided by the sum of the starting materials and the hydrogen-containing combustion gas, in each case in mol./h. Very particularly preferably, 2<lambda<5.
Separation of the powder from the reaction mixture is generally preceded by a cooling process. This process may be carried out directly, for example by means of a quenching gas, or indirectly, for example via external cooling.
The cerium oxide powder may contain impurities resulting from the starting material and/or the process. The purity of the annealed cerium oxide powder is at least 98 wt. %, generally at least 99 wt. %. A content of at least 99.8 wt. % may be particularly preferred.
In general, the cerium oxide powder is predominantly or exclusively in the form of aggregates of primary particles, the aggregates exhibiting no cenospherical structures. A cenospherical structure is to be understood as being a structure that has a size of from 0.1 to 20 μm and is approximately in the form of a hollow sphere, with a wall thickness of from 0.1 to 2 μm. Predominantly is to be understood as meaning that a TEM picture shows individual non-aggregated particles in an amount of not more than 10%.
The cerium oxide powder may preferably have a BET surface area of from 30 to 200 m2/g.
The content of coarse particles >45 μm in the cerium oxide powder is preferably less than 100 ppm and particularly preferably less than 50 ppm.
The cerium oxide powder preferably has a carbon content of less than 0.15 wt. % and a content of chloride, sodium and potassium of less than 300 ppm.
The cerium oxide powder may preferably be a cerium oxide powder having a BET surface area of from 30 to 90 m2/g.
The cerium oxide powder when exposed to air and temperatures of 900° C. for a period of two hours, may have a BET surface area of up to 35 m2/g.
The mean primary particle diameter of the cerium oxide powder may be preferably from 5 to 20 nm and particularly preferably from 8 to 14 nm.
The mean aggregate diameter of the cerium oxide powder may be from 20 to 100 nm and particularly preferably from 30 to 70 nm.
The ceria can be a polycrystalline cerium oxide powder in the form of aggregates of primary particles, which is characterised in that
As used herein, the term “polycrystalline” means that the primary particles are crystalline and fused into aggregates. The term “primary particles” means particles that are initially formed in the reaction and fuse together to form aggregates as the reaction progresses. The term “aggregate” means primary particles of similar structure and size that have fused together, the surface of which is smaller than the sum of the individual, isolated primary particles.
The average primary particle diameter and the average projected aggregate diameter (ECD; Equivalent Circle Diameter) are obtained by image analysis of TEM photographs. Both sizes are defined as number-based within the meaning of the application.
A powder with a specific surface of between 90 and 120 m2/g may be preferred.
The average primary particle diameter can be between 8 and 15 nm and the average projected aggregate diameter between 30 and 70 nm.
It has proved advantageous for the primary particle diameters to have a narrow distribution. This means that, for an average value m of the diameter, at least 68% of the particles are in the range of 0.6 m to 1.4 m or 95% of the particles are in the range of 0.2 m to 1.8 m. For an average primary particle diameter of 10 nm, this means that at least 68% of the particles are in a range of between 6 and 14 nm, or 95% of the particles are in a range of between 2 and 18 nm.
Similarly, it is advantageous if the aggregate diameters have a narrow distribution. This means that, for an average value m of the projected aggregate diameter, at least 68% of the projected aggregate diameters are in the range of 0.6 m to 1.4 m or 95% of the particles are in the range of 0.2 m to 1.8 m. For an average, projected aggregate diameter of 40 nm this means that at least 68% of the particles are in a range of between 24 and 56 nm, or 95% of the particles are in a range of between 8 and 72 nm.
Preferably at least 70%, particularly preferably at least 80% of the aggregates of the cerium oxide powder according to the invention can have an area of less than 1500 nm2.
It is also preferred that at least 85%, particularly preferably at least 90%, of the aggregates of the cerium oxide powders according to the invention have an area of less than 4500 nm2.
In another embodiment, the cerium oxide powder according to the invention can have a composition CeOx with x=1.5<x<2 on the surface, wherein the range 1.7≦x≦1.9 may be particularly preferred. This means that areas of cerium(III) oxide (Ce2O3) and cerium(IV) oxide (CeO2) are present on the surface. This composition may be important particularly in the field of catalysis (oxygen storage, oxygen generation).
The cerium oxide powder according to the invention can have a total sodium content of less than 500 ppm, particularly preferably of less than 100 ppm, especially preferably less than 30 ppm.
In a particular form, the cerium oxide powder according to the invention can have less than 10 ppm on the surface and on layers of the particles close to the surface. This can be determined e.g. by large-area (1 cm2) XPS analysis (XPS=X-ray induced photoelectron spectroscopy). A layer close to the surface means a surface produced by ion bombardment (5 keV argon ions).
In addition, the cerium oxide powder according to the invention can have a carbon content of less than 0.1 wt.-%, particularly preferably of less than 0.05 wt.-%. Sources of carbon are mainly organic cerium oxide precursors and organic solvents.
In one embodiment, the cerium oxide powder according to the invention is free from micropores with a pore diameter of less than 2 nm, determined by t-plot according to de Boer. The volume of the mesopores with a diameter of between 2 and 50 nm in the cerium oxide powder according to the invention can be between 0.40 and 0.60 ml/g, particularly preferably between 0.45 and 0.55 ml/g.
The mesopores in the cerium oxide powder according to the invention preferably exhibit a monomodal size distribution. This means that, when the pore volume is plotted against the pore diameter, no marked maximum (point without slope) occurs in the range between 2 and 50 nm. The pore volume thus increases constantly with the pore diameter.
The invention further provides a process for the production of the cerium oxide powder according to the invention, which is characterised in that an aerosol is reacted in a flame burning in a reaction chamber and the solid obtained is then separated from the gaseous substances, wherein
The cerium oxide powder according to the invention is obtained by a combination of the above-mentioned features. If individual features lie outside the limits claimed, this leads to a cerium oxide powder with an unfavorable, large aggregate diameter and/or to the formation of a coarse portion. A composition of this type cannot be tolerated e.g. when the cerium oxide powder is to be used as an abrasive in the semiconductor industry.
The proportion of the cerium compound in the solution is between 2 and 40 wt.-% in the process according to the invention. Lower values make no sense economically, and with higher values there can be problems with the solubility. It can be advantageous to select a proportion of the cerium compound in the solution of between 5 and 25 wt.-%.
The nature of the solvent, whether aqueous, organic or aqueous-organic, is not limited in the process according to the invention. It is dependent on the solubility of the cerium compounds used. However, it may be advantageous to use an organic solvent or mixtures of organic solvents with water. For example, alcohols such as ethanol, propanols or butanols or carboxylic acids such as acetic acid, propionic acid, 2-ethylhexanoic acid can be used. Halogen-containing solvents can also be used, but they mean that product purification steps are additionally necessary and so they are less advantageous.
The nature of the cerium compounds used in the process according to the invention is not limited. Organic cerium compounds can preferably be used. These can be, for example, cerium alkoxides, such as cerium isopropylate, cerium acetate, cerium acetylacetonate, cerium oxalate, cerium 2-ethylhexanoate and mixtures of the above. Cerium 2-ethylhexanoate can particularly preferably be used.
The solution can be fed in under a pressure of 1 to 1000 bar, preferably between 2 and 100 bar.
The atomization of these solutions can be performed e.g. by ultrasonic atomizer or at least one multi-substance nozzle. The multi-substance nozzle can be used at pressures of up to 100 bar. When a multi-substance nozzle is used, there is the advantage that the droplets can be produced with a gas jet. If this gas jet contains oxygen, a very intensive premixing of the oxidising agent with the cerium-containing compound can be achieved. A mist eliminator can advantageously be connected downstream.
An essential feature of the process according to the invention is the maintaining of the factor lambda, which, in the process according to the invention, is between 1.1 and 1.5. Outside this range, no cerium oxide powder according to the invention is obtained. With lower lambda values, there is the risk of incomplete oxidation, and with higher lambda values, mainly powders containing a coarse portion result. A lambda value of between 1.2 and 1.5 has proved advantageous.
A coarse portion is also obtained if the discharge velocity of the liquid droplets from the atomizer unit into the reaction chamber and the velocity of the reaction mixture in the reaction chamber lie outside the claimed limits.
The term “coarse portion” as used herein refers to particles with an average diameter of more than 100 nm.
Another important feature of the process according to the invention is the quantity of secondary air introduced into the reaction chamber. This must at least correspond to the quantity of primary air to obtain the cerium oxide powder according to the invention. If smaller quantities of secondary air are fed in, an increased proportion of coarse portions must again be expected. A process in which double the quantity of primary air is fed in as secondary air has proved advantageous.
It can also be advantageous if a restrictor is provided in the reaction chamber. This can be positioned at various points in the reaction chamber. With this, the degree of mixing of the reaction components, and the velocity thereof, can be intensified. In general, a turbulent flow will be particularly preferred.
The process according to the invention can be carried out in such a way that the reaction mixture is cooled to temperatures of 100 to 200° C. after leaving the reaction chamber. This can be achieved by introducing water vapor into the reaction chamber at one or more points.
The separation of the solid from gaseous products is not limited in the process according to the invention. For example, a cyclone or a filter can be used. It has proved particularly advantageous to use a heatable filter. The temperature of this filter can preferably be between 100° C. and 200° C.
The temperature in the reaction chamber, measured 0.5 m below the flame, can preferably be between 1000° C. and 1400° C., particularly preferably between 1100° C. and 1250° C.
The goldcatalyst according to the invention can be produced by the method, which is characterized in that a solution of a gold salt i.e. HauCl4 is added into a solution, which contains the suspended support, whereby the temperature is maintained at 60 to 70° C., after aging a time the precipitate is filtered and washed until no Cl-ions were detected, dried and then calcined.
The drying can be made at a temperature of 70 to 90° C. The calcination can be made by a temperature of 100 to 200° C.
The goldcatalyst according to the invention can be used for the oxidation of Co in a H2-stream.
The specific surface is determined in accordance with DIN 66131, incorporated herein by reference.
The TEM photographs are obtained with a Hitachi TEM instrument, model H-75000-2. Using the CCD camera of the TEM instrument and subsequent image analysis, approx. 2000 aggregates are evaluated in each case with respect to the primary particle and aggregate diameters.
The surface properties, such as sodium content and stoichiometry of the cerium oxide powder, are determined by large-area (1 cm2) XPS analysis (XPS=X-ray induced photoelectron spectroscopy).
The stoichiometry of the cerium oxide powder here is determined on the surface in the original state based on the fine structures of the Ce 3d5/2 and 3d3/2.
The sodium content is determined both in the original state and after 30 minutes surface erosion by ion bombardment (5 keV argon ions).
Sodium content (wet chemical): decomposition with H2SO4/HF, determination by ICPMS.
The pore size distribution is determined for micropores (<2 nm) by t-plot according to de Boer, for mesopores (2-50 nm) by the BJH method and for macropores (>50 nm) by Hg intrusion.
The dispersions are produced by ultrasonic treatment; ultrasound probe (Bandelin UW2200/DH13G), step 8, 100%; 5 minutes) in water. The average aggregate diameters d50 of the cerium oxide powders are determined with an LB-500 particle size analyzer from Horiba.
1200 g/h of a solution of cerium(III) 2-ethylhexanoate (49 wt.-%) in 2-ethylhexanoic acid (51 wt.-%) are atomized through a nozzle with a diameter of 0.8 mm into a reaction chamber using air (5 m3/h). Here, an oxyhydrogen gas flame consisting of hydrogen (10 m3/h) and primary air (10 m3/h) is burning, in which the aerosol is reacted. In addition, 20 m3/h of secondary air are introduced into the reaction chamber. A restrictor with a length of 150 mm and a diameter of 15 mm, through which the reaction mixture is passed, is installed in the reaction chamber below the flame. After cooling, the cerium oxide powder is separated from gaseous substances using a filter.
Examples 2 to 4 are performed in the same way as Example 1; the quantities used and other process parameters can be taken from Table 1. In Example 5, no restrictor is employed and cerium(III) nitrate is used instead of cerium(III) 2-ethylhexanoate.
The physico-chemical data of the cerium oxide powders obtained can be taken from Table 2.
The naming of the dispersions corresponds to the relevant powders. Dispersion D1 corresponds to the powder P1 from Example 1, D2 corresponds to P2, etc.
a)Temperature 1 = 0.5 m below the flame,
b)Temperature 2 = reactor outlet
c)cerium(III) nitrate instead of Ce(III) 2-ethylhexanoate;
a)XRD phase: cubic;
b)as 4% solution;
a)Content of cerium oxide: 2 wt.-%
Deposition-precipitation method was used to prepare Au/CeO2 and Au/CexMn1-xO2 catalyst. CO oxidation reaction at room temperature and selective CO oxidation reaction in hydrogen stream at various temperatures were used to test the activity of catalyst.
Two kinds of supports were used in this study, CeO2 and Ce—Mn—O2CeO2 was from Degussa AG. Ce1-xMnxO2 support was prepared by impregnation method. Mn(NO3)2 was added into distilled water equal-volume to CeO2 we took. The solution was added into CeO2 powder dropwise under vigorous grinding. After calcining for two hours at 400° C. for 2 hours, The Ce1-xMnxO2 could be obtained. The sample C-(10*x)Mn means that the support is Ce1-xMnxO2. For example, C-1Mn means that the support is Ce0.9Mn0.1O2.
The CeO2 from Degussa AG has the following chemical-physical datas:
HAuCl4 solution (1 g in 1 liter distilled water) was added with the rate 10 ml/min into the solution containing suspended support under vigorous stirring and the precipitation temperature of solution was maintained at 60 to 70° C. The ammonia solution was used to adjust the pH value at 8. After aging for 2 hours, the precipitate was filtered and washed with hot water until no Cl− was detected with AgNO3 solution, then was dried at 80° C. overnight. The cake was calcined at 120 and 180° C. for several hours to obtain gold catalysts.
The surface areas of supports contained manganese were measured by ASAP 2010. The results are listed in Table 1. Addition of manganese decreased the surface area of CeO2.
XPS analysis was used to determine the oxidation state of gold in this study.
Catalytic activity was measured with a fixed bed continuous flow reactor. Samples were placed in a class column, and no pretreatment was applied in this test. 0.05 cm3 catalysts were used. The reactant gas containing 1000 ppm CO, 2% O2 and N2 else was admitted at the flow rate of 50 cc/min through the reactor. The flow rates were monitored by mass flow controllers. The reaction was occurred at room temperature (25° C.). A CO sensor was used to detect the output CO concentration. The CO conversion was calculated with the following equation:
The catalytic activity was measured in a glass downward, fixed-bed continuous-flow reactor, with 0.1 cm3 catalysts. The reactant gas containing 1.33% CO, 1.33% O2, 65.33% H2 and He for balance was guiding into the reactor with the flow rate of 50 cc/min. The reactor was heated with a regulated furnace (heating rate: 1° C./min) and the temperature was measured by thermocouple placed inside the catalysts bed. The outlet gas was analyzed by a gas chromatography equipped with a thermal conductivity detector. The GC column was MS-5A. Calibration was done with a standard gas containing known concentrations of the components. The CO conversion and selectivity were calculated as follows:
Table 2 lists the reaction results.
Table 3 shows the results according to the art.
The XRD patterns of
(Au-180 means the catalyst was calcined at 180 degree Celsius.)
The XRD patterns of
The XRD patterns of
TEM images of gold catalysts calcined at different temperatures supported on Adnano Ceria.
TEM images and size distribution of gold of catalysts supported on C-1Mn.
TEM images and size distribution of gold of catalysts supported on C-5Mn.
XPS results of gold calcined at different temperatures supported on Adnano Ceria 90.
XPS results of gold calcined at different temperatures supported on C-1Mn.
XPS results of gold calcined at different temperatures supported on C-5Mn.
CO conversion (%)
CO conversion of gold catalysts supported on Adnano Ceria.
The Au catalysts were prepared by deposition-precipitation method using NH4OH and HAuCl4, synthesized at pH 8 and calcined at 120 and 180° C. in air.
Catalyst sample: 0.05 cm3 of 1 wt. % Au/CeO2. Reactant gas: 1000 ppm CO, 2% O2 and N2 for balance, 50 ml/min,
GHSV=60,000 h−1. The catalytic activity was measured at ambient temperature about 25° C.
Selective CO oxidation reaction results of gold catalysts supported on Adnano Ceria 90 calcined at 120 and 180° C.
The Au catalysts were prepared by deposition-precipitation method using NH4OH and HAuCl4, synthesized at pH 8.
Catalyst sample: 0.1 cm3.
Reactant gas: 1.33% CO+1.33% O2+65.33% H2+He for balance, 50 ml/min,
GSHV=30,000 h−1.
Selective CO oxidation reaction results of gold supported on Ce—Mn—O and calcined at different temperatures.
The Au catalysts were prepared by deposition-precipitation method using NH4OH and HAuCl4, synthesized at pH 8.
Catalyst sample: 0.1 cm3.
balance, 50 ml/min,
GSHV=30,000 h−1.
| Number | Date | Country | Kind |
|---|---|---|---|
| 05011050.1 | May 2005 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2006/061628 | 4/18/2006 | WO | 00 | 5/14/2008 |
