Process and system for the removal of nitrogen oxides using a catalytic membrane

Abstract: A lean-NO x catalyst having a sol-gel processed membrane. The sol-gel processed membrane is loaded with a transition metal. Methods are also disclosed for loading a transition metal on the membrane and reducing emissions in an exhaust stream to provide a NO x reduction system which can operate in a broad range of operating conditions.

Description: This invention relates to lean-NO x catalysts, particularly those providing a high surface area catalyst membrane of controlled pore size to remove nitrogen oxide (NO x ) emissions from lean-burn automobile engines and industrial plants emission systems. The present invention also discloses a method of making such catalysts. The Environmental Protection Agency has instituted stringent automobile-related environmental regulations. A primary focus of the regulation relates to the Corporate Average Fuel Economy (CAFE) standards, which mandate a specified, gradual increase of a corporate fleet's overall fuel economy by the established target dates. CAFE standards have spurred industry wide research and development of "lean-burn engines". The term "lean-burn engine" used herein is defined as an engine utilising air/fuel mixtures having an oxygen content in excess of the stoichiometric air/fuel ratio (lean mixtures). The use of such lean air/fuel mixtures, reduces the consumption of fuel and thus enhances an automobile's fuel economy. The effort to increase automobile fuel economy has become paramount in the wake of the Environmental Protection Agency's tightening CAFE standards. In addition to the CAFE standards, the Environmental Protection Agency has set a schedule for the continual reduction of specific automotive emissions. Thus, the Environmental Protection Agency's regulatory measures have required the automobile industry to simultaneously increase fuel economy while decreasing harmful exhaust emissions. Accordingly, there exists a new found interest in the development of a catalyst to operate efficiently under lean-burn conditions. Many of the prior art catalysts were designed to optimally operate at or about stoichiometric conditions. These prior art catalysts when combined with a lean fuel mixture result in O 2 being adsorbed by the catalyst, preventing NO x from being reduced to nitrogen (N 2 ) by the active metal on the catalyst. So while the current three-way catalyst, for example, may effectively reduce NO, hydrocarbons (HC) and CO emissions at stoichiometric conditions, the efficiencies of a three-way catalyst for NO x reduction diminish significantly in an oxygen rich environment. The effectiveness of a catalyst is largely dependent on the air/fuel ratio of the fuel mixture which is employed in an engine. If a lean mixture is utilised, a catalyst exhibits a high activity of oxidation but a low activity of reduction, while the combustion product contains a large amount of oxygen. In contrast, in the presence of a fuel rich mixture, a catalyst exhibits a high activity of reduction but a low activity of oxidation. At stoichiometric air/fuel ratios, oxidation and reduction are balanced. Accordingly, there is a need for a lean-NO x catalyst which efficiently reduces NO x emissions in the presence of a lean fuel mixture. In addition to automotive applications, lean-NO x catalysts are also valuable in lowering the emissions of stationary power plants that burn fossil fuels. A lean-NO x catalyst is defined for purposes of this application as a catalyst that can reduce NO x under lean-burn conditions. In answer to this problem, transition metal-containing zeolite catalysts have been developed to reduce NO x emissions for lean mixtures. In particular, copperzeolite catalysts have been preferred due to the effectiveness of copper as an ion exchange metal at lower temperatures such as that present in lean-burn engine exhaust. Zeolites are crystalline aluminosilicates. Zeolites are commercially available and are characterised by crystal structures having different channels or pore diameters. Zeolites have fine pores (sized at several angstroms), comparable with the size of a molecule, hence they are termed molecular sieves. It is believed that the hydrocarbons are selectively trapped in those pores or sieves. As the transition metal, introduced by ion exchange, forms active sites in the pores, the hydrocarbons are adsorbed therein and react with nitrogen oxides in the presence of excess O 2 . Accordingly, zeolite catalysts have potential application in the removal of NO x from lean fuel mixtures. The basic principle behind removing NO x in a lean fuel mixture with a transition metal, e.g., copper, containing zeolite catalyst relies on adsorbing NO x and effectuating a catalytic reaction of the adsorbed NO x with the hydrocarbons contained in the exhausted gas, to reduce the NO x to N 2 . Although copper-zeolite catalysts have good catalytic activity initially, due to copper's high NO x adsorption ability, copper-zeolite catalysts have a series of limitations which are described below. First, transition metal containing zeolites degrade at high temperatures usually found in automotive exhaust systems. Furthermore, if the zeolite catalyst is exposed to steam-containing air, e.g., automotive exhaust, the activity of the catalyst decreases rapidly. The decrease in activity is also accompanied by dealumination. Steam deactivation of zeolite-based catalysts is the primary reason why such catalysts are not practical in application. To compensate for the problems associated with zeolites, alumina (Al 2 O 3 ) has been used in three-way catalysts as support for active ingredients. The use of Al 2 O 3 and metal containing Al 2 O 3 as lean-NO x catalysts has been reported by H. Hamada, Y. Kintaichi, M. Sasaki and T. Ito in "Transition metal-promoted silica and alumina catalysts for the selective reduction of nitrogen monoxide with propane", Applied Catalysts , L1-L8 (1991). Alumina, however, is inefficient in NO x reduction such that it is currently impractical for commercial use. Thus, a need exists for a commercially practical, efficient, lean-NO x catalyst. According to the invention a catalyst comprising an alumina or alumina/silica membrane produced by a sol-gel process, having a pore size distribution in the range of 20-60 angstroms and being loaded with one or more of the transition metals iron, copper, cobalt, chromium, silver, nickel and manganese is used in a process for removing nitrogen oxide (NO x ) emissions from oxygen-rich combustion gases, in particular those forming the exhaust stream of a lean-burn vehicle engine. The production of alumina membranes by sol-gel processes is described in US-A 5 210 062, and that specification also discloses the use of such membranes impregnated with precious metals such as palladium, platinum, rhodium and iridium as catalysts for the treatment of automobile exhaust gases. However, these metals are poor lean-NO x catalysts. The use of ceramic membranes consisting of metal oxides such as TiO 2 and ZrO 2 or oxides of silicon, aluminium, niobium or other transition metals and made by a sol-gel process in separation processes is also disclosed in EP-A 0 425 252, but there is no suggestion therein of loading the ceramic membrane with transition metal or using it as in the present invention. DE-A 43 03 610 discloses the use in heterogeneous catalysed reactions such as the hydrogenation of linoleic acid dimethyl ester of microporous membranes produced by a sol-gel process and containing a wide variety of catalytically active components. In these reactions two reagents are separated by the membrane, which is permeable to one reagent but not permeable to the other reagent or to impurities contained therein. The invention also provides an emission reduction system as set forth in claim 8. It further provides a NO x reduction system for catalytic reduction under lean-burn conditions in an automobile exhaust stream in which the aforesaid alumina or alumina/silica sol-gel lean-NO x catalyst is combined with a three-way catalyst to provide an emission system which can operate over a broad range of operating conditions. The instant invention has many advantages. First, the sol-gel process provides inorganic membranes which have customised pore sizes. This flexibility allows the inorganic membranes to in effect mimic the effectiveness of the zeolite pore structure. Second, alumina/silica membranes retain high surface area even after high temperature treatment. Third, these alumina/silica membranes are thoroughly stable high surface area membranes. The resulting catalyst membrane can thereby have significantly increased hydrothermal stability the consequent improved performance. The invention will now be described further, by way of example, with reference to the accompanying drawings, in which: Fig. 1 is a graphic comparison of NO conversion efficiency between an Ag-containing sol-gel processed membrane catalyst and a Cu/ZSM-5 catalyst; Fig. 2 is a graphic comparison of NO conversions between an Ag-containing sol-gel processed membrane catalyst and a commercially available Ag on Y-alumina catalyst; Fig. 3 depicts three embodiments of an emission reduction system, wherein in Fig. 3A a catalytic converter containing an Ag/sol-gel processed alumina membrane is positioned in the exhaust stream of an IC engine, in Fig. 3B this catalytic converter is followed by a three-way catalyst (TWC), and in Fig. 3C two lean-NO x catalysts, namely an Ag/sol-gel processed alumina catalyst and a zeolite catalyst, are used in conjunction with a three-way catalyst. Zeolite membranes are characterised by their crystalline structure. In contrast, sol-gel processed alumina or alumina/silica membranes are amorphous unless sintered at high temperature and are prepared from a sol composition, i.e. a liquid colloidal dispersion. A sol in this case is a gel which comprises highly-cross-linked inorganic polymers. A sol can be converted to gel by several known methods such as concentrating the sol, heating or cooling the sol. These alumina sols can be employed to prepare alumina membranes for use on ceramic monoliths as described in US-A 5 210 062. In the preferred embodiment, alumina sols were prepared by hydrolysing aluminium alkoxides in water followed by peptisation in the presence of dilute mineral acid. The silica sol was concentrated to a gel which was then heated at 250°C and 600°C in a nitrogen atmosphere. The sol was prepared from Si(EtO) 4 in ethanol, water and dilute mineral acid. Alumina membranes which were then prepared from alumina sols showed a surface area of 230 m 2 /g and pore size of 45 angstroms after heating at 600°C. Alumina/silica membranes which were prepared from a mixture of alumina and silica sol and aged at 600°C showed a surface area of 390 m 2 /g and pore size of 45 angstroms. Alumina/silica membranes prepared by treating alumina membranes with silica sol show pore sizes of 30 and 40 angstroms. In another embodiment, alumina/silica materials were prepared from (tBuO) 3 Si-O-Al(OR) 2 and Al(OR) 3 in parent alcohol. These materials also retained high surface area after aging at 1100°C in air. A transition metal from the group copper, cobalt, nickel, chromium, iron, manganese, silver and zinc was loaded on to the membrane by dissolving a water soluble salt containing the metal in distilled water to form a transition metal containing solution and impregnating the solution on the sol-gel processed membrane material by the following steps: mixing the membrane material and the solution to form a mixture; stirring the mixture; evaporating water from the mixture to form a paste; drying the paste to form a dried sample; and calcining the dried sample. The term transition metal herein includes both the elemental metal itself and its metal oxide. The preferred metal for impregnation on the membrane surface is silver. The silver was impregnated on the membrane by mixing the membrane material and the impregnation solution, stirring the mixture, and slowly evaporating water until the mixture turns pasty. The impregnating solution contained the known amount of silver nitrate and 5-10 volume percent of concentrated nitric acid. The paste was then dried at 50°C overnight and for at least 4 hours at 120°C. The dried sample was finally calcined at 550°C for 4 hours. The efficiency for lean-NO x reduction was measured under a model reaction condition. A result showed that 80% NO was reduced to nitrogen at 450° to 525°C. The ratio of the amount of transition metal to the weight of the sol-gel processed membrane is dependent on the desired transition metal loading on the sol-gel processed material. When the transition metal is silver, the amount of silver supported on the membrane is generally in the range of 1-8 weight percent of the overall weight. Generally, however, the amount of the transition metal is in the range of 1-20 weight percent of the overall weight. The sol-gel processed alumina used has a pore size distribution in the range of 20-60 angstroms. As a result of this ability to control the porosity of the membrane, silver or any other transition metal deposited in these pores has a high surface area, resulting in a membrane with high activity. Alumina sols were prepared by hydrolysing aluminium alkoxides (e.g. Al(OBu S ) 3 ) in water followed by peptisation in the presence of diluted mineral acid. The sol was then concentrated to gel which was then heated at 250°C and 600°C in a nitrogen atmosphere. Alumina/silica membranes were prepared from a mixture of aluminium sol and silica sol which was obtained from Si(EtO) 4 in ethanol, water, and diluted mineral acid. A sample of alumina/silica membrane was made with uniform pore size around 45Å and 390m 2 /g. Two samples of sol-gel processed alumina membrane material, SG1 (195 m 2 /g and 40 Å-pore) and SG2 (224 m 2 /g and 39 Å-pore), were used in the following disclosure. Water-soluble Ag-containing salts such as AgNO 3 were dissolved in distilled water. The Ag-solution was then used to impregnate the sol-gel processed membrane material. The ratio of the Ag amount to the membrane weight was dependent on the desired Ag loading on the sol-gel processed material. After the impregnation, the material was dried up to 120°C and then heated in air inside a furnace at 500-600°C for 4 hours. EXAMPLES The present invention will now be further illustrated by, but in no way limited to the following examples. In the examples listed, unless otherwise indicated, all percents are percents by weight and temperatures cited are in degrees Celsius. ZSM-5, as herein referred to, is a type of zeolite. ZSM-5 is a trademark of Mobil Corporation. It is a siliceous zeolite with a high ratio of SiO 2 to Al 2 O 3 and a high acid strength. ZSM-5 has rings of 10 oxygen atoms, it contains very little water of crystallisation, is hydrophobic and has a few acid sites. Example 1 For CATALYST 1, 2 grams of SG2 (sol-gel processed Al 2 O 3 ) powder was added into a Ag-containing solution which was made of 0.8 ml solution of 4.95 x 10 -2 g Ag/ml, 0.25 ml of concentrated HNO 3 , and 1.85 ml distilled water. Under constant stirring, water was slowly evaporated till the mixture of the powder and the solution turned into paste. The paste was then dried at 120°C overnight and heated at 500°C for 4 hours. Example 2 For CATALYST 2, 2 grams of SG1 powder was used. The solution used for impregnation was the same as that for CATALYST 1. The procedure of preparation was also the same as that for CATALYST 1. Example 3 For CATALYST 3, a sample of CATALYST 2 that was prepared according to the procedure above went through the same impregnation and heating steps again. The resulted loading of Ag on CATALYST 3 was two times of that for CATALYST 2. Example 4 For CATALYST 4, 0.89 gram of CATALYST 1 was added into a solution which was made of 1 ml solution of 0.0178 g Ag/ml and 0.3 ml of distilled water. The water was slowly evaporated till paste was formed. The paste was dried at 110°C for 2 hours. The dried material was again impregnated with the same solution. After drying at 100°C, the sample was heated in air at 525°C for 3 hours. Example 5 For CATALYST 5, 0.91 gram of SG1 was added into a solution which was made of 0.511 ml of 0.0178g Ag/ml solution and 0.8 ml distilled water. Following the slow evaporation of water, the resulted paste was dried at 110°C and finally heated in air at 525°C for 3 hours. Example 6 For CATALYST 6, 10 grams of commercially available γ-Al 2 O 3 used for TWC was added into 15 ml solution containing 0.2066 gram Ag and 0.5 ml concentrated HNO 3 . Under constant stirring, the water was evaporated slowly and the resulted paste was dried at 100°C for 1 hour, 250°C for 1 hour, and finally at 500°C for 5 hours. This catalyst represents the preferred Ag-catalyst using this type of Al 2 O 3 . Example 7 For CATALYST 7, 2 grams of SG2 was added into a solution made of 1.6 ml of 0.0246 g Cu/ml solution, 0.25 ml of concentrated HNO 3 , and 1.65 ml distilled water. After the slow evaporation of water, the material was dried at 120°C and then heated in air at 500°C for 4 hours. This catalyst is Cu-containing sol-gel Al 2 O 3 . Example 8 CATALYST 8 was a commercially available Cu/ZSM-5 catalyst with Si/Al ratio = 19 and 2.9 weight % of Cu. The sample was prepared by a typical ion-exchange method using Cu(II)-acetate and H-ZSM-5 zeolite (Table 1). The obtained sample was heated in air at 550°C for 4 hours. The efficiency was measured under model reaction conditions: 1 - 10 % O 2 , 500 - 1500 ppm C 3 H 6 , 1000 ppm NO, and space velocities equivalent to 12,500 - 50,000 hr -1 . Table 2 shows that CATALYST 1 could reduce NO in range of 3 - 10 % O 2 . Under the same reaction conditions, the efficiency of CATALYST 6 prepared from the commercially available γ-Al 2 O 3 was generally lower than that of CATALYST 1. The efficiencies of CATALYST 1 at different space velocities are shown in Table 3. The NO-reduction efficiency changed slightly in the range of O 2 -concentration or space velocity applied above. The effect of C 3 H 6 -concentration was shown in Table 4. Table 5 shows that CATALYST 7, Cu-containing SG2, can reduce NO at lower temperature than Ag/SG1 or Ag/SG2 under the same conditions. The efficiencies in Table 6 were measured at the conditions similar to those in A above, except that C 3 H 6 was replaced by a mixture of C 3 H 6 and C 3 H 8 with the ratio of C 3 H 6 /C 3 H 8 = 2 which represents the ratio of saturated hydrocarbons to olefins in the automobile exhaust. The maximum efficiencies for CATALYST 1 - 5 with Ag loading from 1 to 6 weight % are shown in Table 6 along with the activities of CATALYST 6 and CATALYST 8. Most Ag/sol-gel processed Al 2 O 3 catalysts had larger activities of NO-reduction. LIST OF CATALYSTS Metal Used Catalyst No. Type Weight% Support 1 Ag 2 SG2 2 Ag 2 SG1 3 Ag 4 SG1 4 Ag 6 SG2 5 Ag 1 SG1 6 Ag 2 γ-Al 2 O 3 7 Cu 2 SG2 8 Cu 2.9 H-ZSM5 NO-CONVERSION AT DIFFERENT LEVEL OF O 2 (1000 ppm NO, 500 ppm, C 3 H 6 , equivalent space velocity = 25,000 hr -1 ) CATALYST O 2 (%) T(°C) NO-Conversion (%) CATALYST 1 3 525 52.2 6 500 54.4 10 500 46.2 CATALYST 6 3 575 31.1 6 550 33.6 10 500 34.2 NO-CONVERSION OVER CATALYST 1 AT DIFFERENT SPACE VELOCITY (1000 PPM NO, 1500 PPM C 3 H 6 , 10% O 2 ) Equivalent Space Velocity T(°C) NO-Conversion (%) 25,000 hr -1 500 83.8 50,000 hr -1 500 76.9 EFFECT OF C 3 H 6 -CONCENTRATION (1000 ppm NO, 10% O 2 , equivalent space velocity = 25,000 hr -1 ) C 3 H 6 -Concentration (ppm) T(°C) NO-Conversion (%) 500 500 46.2 1500 500 83.8 NO-CONVERSION OVER CATALYST 7 (1000 ppm NO, 1500 ppm C 3 H 6 , equivalent space velocity = 25,000 hr -1 ) O 2 (%) T(°C) NO-Conversion (%) 1 475 69.2 3 450 54.8 NO-EFFICIENCY COMPARISON (1,000 ppm NO, 1500 ppm C 3 H 6 , equivalent space velocity = 25,000 hr -1 ) CATALYST No. Description O 2 (%) T(°C) NO-Conversion (%) 5 1 wt% Ag/SG1 10 525 91.6 2 2 wt% Ag/SG1 10 500 96.7 3 4 wt% Ag/SG1 10 475 98.7 4 6 wt% Ag/SG2 10 450 44.8 1 2 wt% Ag/SG2 10 500 95.0 6 2 wt% Ag/γ-Al 2 O 3 10 500 62.6 8 2.9 wt% Cu/ZSM5 6 550 62.8 In a simulated exhaust mixture containing 9% H 2 O and 18 ppm SO 2 1000 ppm NO, 1515 ppm C 3 H 6 and 25,000 hr -1 , the efficiency of NO-reduction for CATALYST 1 was higher than that for CATALYST 6 (Ag on commercial γ-Al 2 O 3 or CATALYST 8 (commercial Cu/ZSM-5) as shown in Figure 1. At 550°C and in the presence of 9% H 2 O and 18 ppm SO 2 1000 ppm NO, 950 ppm C 3 H 6 , 520 ppm C 3 H 6 and 0.51 min -1 the NO-reduction efficiency for CATALYST 1 did not decrease along with time and was higher than that for CATALYST 6 as shown in Figure 2. Catalytic applications using the disclosed sol-gel processed membrane include: 1) Using such a catalyst in stationary power plants and 2) Using a catalyst having a sol-gel processed membrane in conjunction with a three-way catalyst to allow dual catalytic converters to provide comprehensive emission reductions at a broad range of operating temperatures. The three-way catalyst performs effectively at stoichiometric air/fuel ratio to reduce NO x in the lower temperature ranges. Fresh Cu ZSM-5 zeolite catalyst is best suited to operate on the 280-400°C range temperature at lean conditions. Likewise, the sol-gel processed catalytic converter works efficiently for NO x reduction at lean conditions in the 400-550°C temperature range. In application, the combination provides comprehensive conversion efficiency for the reduction of automobile emissions. For example, Fig. 3B illustrates schematically one such NO x reduction system for lean-burn conditions in an automobile exhaust stream, having an upper end near the engine and a lower end near the tail pipe, which includes at least one sol-gel processed alumina or alumina/silica membrane based, lean-burn catalyst in which the substrate is loaded with transition metal (Converter 1) positioned at the upper end of the exhaust stream and a three-way catalyst (TWC) positioned at the lower end of the exhaust stream to provide a system which can operate in a wide range of temperatures. An additional converter (Converter 2) having a zeolite lean NO x catalyst may be included between Converter 1 and the TWC, as shown in Fig. 3C. Preferably, the above systems would include control means for routing exhaust to each type of catalytic converter depending on the air/fuel ratio present. Thus, if the air/fuel ratio is in excess of stoichiometric conditions (14.6) then the exhaust stream should be routed through the inorganic membrane-based lean NO x catalysts, which may be used in conjunction with the copper ZSM-5 lean-NO x catalyst placed at the lower end of the exhaust stream. On the contrary, if the air/fuel ratio is fuel rich or less than 14.6 the exhaust stream should be routed through the three-way catalyst. The control means may comprise monitoring means positioned near the engine to measure the air/fuel ratio of the exhaust stream and control means to alter the exhaust flow depending on the air/fuel ratio as described above. In addition, depending on the particular set of operating conditions, an oxidation catalyst can also be added downstream of the lean-burn catalyst to remove any remaining hydrocarbons which may be present in the emission stream. The above system provides an emission reduction system to cover an automobile's varying air/fuel ratio and a spectrum of operating temperatures while still effectively reducing HC, CO and NO x emissions from an exhaust stream.

Claims: A process for removing nitrogen oxide (NO x ) emissions from oxygen-rich combustion gases by using a catalyst comprising an alumina or alumina/silica membrane produced by a sol-gel process, said membrane having a pore size distribution in the range of 20-60 angstroms and being loaded with one or more of the metals iron, copper, cobalt, chromium, silver, nickel and manganese. A process as claimed in claim 1, wherein the amount of said metal loaded on the membrane is in the range of 1-20 wt % of the overall weight of the membrane. A process as claimed in claim 1 or claim 2, wherein the metal loaded is copper or silver. A process as claimed in claim 3, wherein the metal loaded is silver in the amount of 1-8 wt % of the overall weight of the membrane. A process as claimed in any preceding claim wherein the catalyst is prepared by impregnating alumina or alumina/silica membrane material produced by a sol-gel process by stirring with an aqueous solution of a salt of the metal to be loaded, evaporating to remove water and form a paste, drying said paste and calcining the dried paste. A process as claimed in claim 5, wherein the paste is dried at up to 120°C and calcined at 500-600°C. A process as claimed in any preceding claim, wherein the oxygen-containing gases are exhaust gases from an internal combustion engine operated with a lean fuel mixture. An emission reduction system for catalytic reduction of nitrogen oxides (NO x ) in a vehicle exhaust stream of emissions produced by a lean-burn vehicle engine, said system comprising a lean-burn catalyst positioned in said exhaust stream and comprising an alumina or alumina/silica membrane produced by a sol-gel process, said membrane having a pore size distribution in the range of 20-60 angstroms and being loaded with one or more of the metals iron, copper, cobalt, chromium, silver, nickel and manganese. A system as claimed in claim 8, wherein the amount of said metal loaded on the membrane is in the range of 1-20 wt % of the overall weight of the membrane. A system as claimed in claim 9, wherein the metal loaded is copper or silver. A system as claimed in claim 10, wherein the metal loaded is silver in the amount of 1-8 wt % of the overall weight of the membrane. An emission reduction system as claimed in any of claims 8 to 11, also comprising a three-way catalyst positioned in the exhaust stream such that said lean-burn catalyst is positioned closer to the engine than said three-way catalyst, to provide a system which functions over a broad range of operating conditions. A system as claimed in claim 12, further comprising a zeolite catalyst positioned in the exhaust stream such that said lean-burn catalyst is closer to the engine than said zeolite catalyst. A system as claimed in claim 12 or claim 13, further comprising an oxidation catalyst, positioned in the exhaust stream such that said lean-burn catalyst is closer to the engine than said oxidation catalyst, to substantially remove hydrocarbon emissions from the exhaust stream. A system as claimed in claim 12, further comprising monitoring means positioned near the engine to measure the air/fuel ratio of the exhaust stream and control means to alter the exhaust flow depending on the air/fuel ratio, to provide a way to route the exhaust stream to said lean-burn catalyst if said air/fuel ratio is in excess of stoichiometric air/fuel values or to route the exhaust stream to said three-way catalyst if said air/fuel ratio is equal to or less than stoichiometric air/fuel values.

Inventors: GANDHI HAREN SARKARLAL, JEN HUNG-WEN, NARULA CHAITANYA KUMAR, GANDHI, HAREN SARKARLAL, JEN, HUNG-WEN, NARULA, CHAITANYA KUMAR
Applicants: FORD FRANCE, FORD MOTOR CO, FORD WERKE AG, FORD FRANCE S.A., FORD MOTOR COMPANY, FORD MOTOR COMPANY LIMITED, FORD-WERKE AKTIENGESELLSCHAFT
Application year: 1995
Main classification: B01D53
IPC codes: B01J23, B01D53, B01D71, B01J29