CATALYZED PARTICULATE FILTER FOR SOOT REMOVAL FROM ENGINE EXHAUST

Abstract

The invention discloses use of a catalyzed particulate filter loaded with a silver-zirconia catalyst prepared by citric acid-assisted sol-gel method for soot removal from engine exhaust. The invention discloses a method of making xAg/ZrO.sub.2 where x is 20 mol %, said method comprises: mixing aqueous solutions of AgNO.sub.3 and ZrO(NO.sub.3).sub.2 hydrate to produce a first mixture, adding an aqueous solution of citric acid to the first mixture, wherein the molar ratio of metal ions to citric acid is about 1:3 to produce a second mixture; heating the second mixture to about 80-90° C. to evaporate excess water in the second mixture to form a viscous gel, charring the viscous gel at about 200° C. for about 12 hours to produce a foam-like material, grounding the foam-like material to form a grounded material, and calcinating the grounded material at 500° C. for about 10 hours.

Claims

1. Use of a catalyzed particulate filter, said particulate filter is loaded with a silver-zirconia catalyst, for soot removal from engine exhaust, wherein the silver-zirconia catalyst is prepared by citric acid-assisted sol-gel method.

2. The use according to claim 1, wherein the silver-zirconia catalyst is xAg/ZrO.sub.2, where x is the mole fraction of Ag in %, wherein the Ag content x is 5-30 mol %.

3. The use according to claim 2, wherein Ag content x is 20-30 mol %.

4. The use according to claim 2, wherein Ag content x is Ag content x is 30 mol %.

5. The use according to claim 2, wherein Ag content x is 20 mol %.

6. The use according to claim 1, wherein the soot removal from engine exhaust is for lean-burn internal combustion.

7. A method of making a catalyst xAg/ZrO.sub.2 where x is 20 mol %, said method comprises: mixing aqueous solutions of AgNO.sub.3 and ZrO(NO.sub.3).sub.2 hydrate to produce a first mixture, adding an aqueous solution of citric acid to the first mixture, wherein the molar ratio of metal ions to citric acid is about 1:3 to produce a second mixture, heating the second mixture to about 80-90° C. to evaporate excess water in the second mixture to form a viscous gel, charring the viscous gel at about 200° C. for about 12 hours to produce a foam-like material, grounding the foam-like material to form a grounded material, and calcinating the grounded material at 500° C. for about 10 hours.

8. Use of a catalyzed particulate filter, said particulate filter is loaded with a silver-zirconia catalyst made according to claim 7, for soot removal from engine exhaust.

9. The use according to claim 8, wherein soot removal from engine exhaust is for lean-burn internal combustion.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0039] By way of example only, preferred embodiments of the present invention are described hereinafter with reference to the accompanying drawings, wherein:

[0040] FIG. 1 shows the Temperature Programmed Oxidation (TPO) profile for 30Ag/ZrO.sub.2 catalyst for carbon oxidation (10 vol % O.sub.2/He, tight contact, catalyst:carbon ratio=30:1).

[0041] FIG. 2 shows the carbon dioxide concentration versus temperature profiles for 20Ag/ZrO.sub.2 (calcined at 500° C., 10 h) and 30Ag/ZrO.sub.2 (calcined at 550° C., 6 h) tested with 10 vol % O.sub.2, 5 vol % H.sub.2O, 500 ppm NO in N.sub.2 and under tight contact mode.

[0042] FIG. 3 shows the schematic of a wall-flow Ag/ZrO.sub.2 catalyzed particulate filter with an enlarged view of a channel.

[0043] FIG. 4 shows the schematic of an engine test setup of an Ag/ZrO.sub.2 catalyzed particulate filter.

[0044] FIG. 5 shows the pressure changes during engine testing of a catalyzed filter wherein the filter is an Ag/ZrO.sub.2 catalyzed particulate filter according to the present invention.

[0045] FIG. 6 shows the pressure changes during engine testing of a catalyzed filter wherein the filter is the same as used in commercial base metal-palladium “Cattrap” CDPF.

[0046] FIG. 7A shows a CDPF progressive load test: CDPF inlet temperature versus engine load at peak torque speed. FIG. 7B shows differential pressure and CDPF inlet temperature versus time.

[0047] FIG. 8A shows CO emissions as a function of inlet temperature as measured at the CDPF inlet and outlet ports, and FIG. 8B shows the % change in CO concentration under testing conditions.

[0048] FIG. 9A shows the Total Hydrocarbons (THC) emissions as a function of inlet temperature as measured at the CDPF inlet and outlet ports, and FIG. 9B shows the % change in THC concentration under testing conditions.

[0049] FIG. 10 shows NO emissions as a function of inlet temperature as measured at the CDPF inlet and outlet ports.

[0050] FIG. 11A shows NO.sub.2 emissions as a function of inlet temperature as measured at the CDPF inlet and outlet ports, and FIG. 11B shows the % change in NO.sub.2 concentration under testing conditions.

[0051] FIG. 12 shows PM emissions tested during 8-mode testing cycle and PM reduction efficiency.

DETAILED DESCRIPTION OF THE INVENTION

[0052] It is to be understood that the disclosure is not limited in its application to the details of the embodiments as set forth in the following description. The invention is capable of other embodiments and of being practiced or of being carried out in various ways.

[0053] Furthermore, it is to be understood that the terminology used herein is for the purpose of description and should not be regarded as limiting. Contrary to the use of the term “consisting”, the use of the terms “including”, “containing”, “comprising”, or “having” and variations thereof is meant to encompass the items listed thereafter and equivalents thereof as well as additional items. The use of the term “a” or “an” is meant to encompass “one or more”. Any numerical range recited herein is intended to include all values from the lower value to the upper value of that range.

[0054] The present invention discloses a catalyzed particulate filter, which uses the silver-zirconia catalyst supported on porous cordierite wall-flow substrate and performs passive regeneration at lower temperatures than that of a commercial base metal-palladium filter.

[0055] The catalyst formulation comprising silver supported on tetragonal zirconia was developed, thoroughly characterized and optimized.

[0056] Unlike the commercial CRT technology, the present invention discloses a new and less expensive silver-based catalyzed particulate filter, which offers low temperature oxidation of collected particulate matter performing continuous passive regeneration of the filter.

Effect of Calcination Temperature on Catalytic Properties of Ag/ZrO.SUB.2 .Catalysts

[0057] An improved version of the 30Ag/ZrO.sub.2 catalyst was developed with a significantly lower content of silver (decrease of 33%). This was achieved by changing the calcination procedure.

[0058] The effect of calcination temperature on the physical and chemical properties of 20Ag/ZrO.sub.2 and 30Ag/ZrO.sub.2 catalysts prepared by the same citrate sol-gel method was studied to determine the optimum pre-treatment conditions.

[0059] Table 1 below presents the physical characteristics for the catalysts pretreated at different conditions.

TABLE-US-00001 TABLE 1 Physical characteristics of Ag/ZrO.sub.2 catalysts calcined at different conditions 20Ag/ZrO.sub.2 30Ag/ZrO.sub.2 500° C. 550° C. 500° C. 550° C. Physical Characteristics (10 h) (6 h) (10 h) (6 h) Surface BET Area (m.sup.2/g) 32.0 21.4 19.5 18.2 Pore Volume.sup.a (cm.sup.3/g) 0.18 0.15 0.12 0.13 Ag Particle Size.sup.b (nm) 18.9 27.5 29.8 44.8 Ag Surface Area.sup.b (m.sup.2/g Ag) 30.2 20.8 19.2 12.7 .sup.aBJH desorption cumulative pore volume .sup.bCalculated from O.sub.2-chemisorption data

[0060] As seen from Table 1, the change in calcination temperature from 550° C. for 6 h to 500° C. for 10 h caused an increase of the BET surface area of both catalysts and the pore volume of 20 Ag/ZrO.sub.2 catalyst.

[0061] The increase was markedly larger for the 20Ag/ZrO.sub.2 catalyst showing 32.0 m.sup.2/g surface area and 0.18 cm.sup.3/g pore volume, respectively.

[0062] On the other hand, this effect for the 30Ag/ZrO.sub.2 catalyst was significantly less pronounced as indicated by only a slight increase in its surface area from 18.2 m.sup.2/g to 19.5 m.sup.2/g.

[0063] Additionally, the new and improved calcination procedure influenced the Ag particle size and consequently the Ag surface area exposed to the reactants during reaction.

[0064] Table 1 shows Ag particle size of the 20Ag/ZrO.sub.2 catalyst that significantly decreased from 27.5 nm to 18.9 nm giving rise to a higher specific Ag surface area of 30.2 m.sup.2/g compared to 20.8 m.sup.2/g when the higher calcination temperature was used.

[0065] The calcination temperature influenced the sintering of Ag particles in the 30Ag/ZrO.sub.2 catalyst exhibiting smaller Ag particle size of 29.8 nm when calcined at 500° C. versus 44.8 nm after 550° C. calcination. Corresponding specific Ag surface area of 19.2 m.sup.2/g Ag versus 12.7 m.sup.2/g Ag were measured, respectively.

[0066] Larger surface area and pore volume can provide more active sites for gaseous reactants adsorption and activation and for building more contact points with soot particles.

[0067] Therefore, the calcination at 500° C. for 10 h reduced the degree of support and Ag sintering and affected pore properties advantageous to the reaction.

[0068] The catalytic properties of the catalysts calcined at different conditions were evaluated using TPO experiments with 10 vol % O.sub.2/He.

[0069] The testing sample consisted of a mixture of a catalyst with carbon black in tight contact mode and weight ratio of 30:1. The change in combustion product (CO.sub.2) concentrations as a function of temperature during TPO runs were measured by using a thermal conductivity detector (TCD) detector.

[0070] The catalytic performance was assessed by values of the temperature at the maximum carbon oxidation rate (T.sub.max) that corresponded to the peak temperature in TPO profiles. A lower T.sub.max indicated a greater catalytic activity.

[0071] A typical profile of the 30Ag/ZrO.sub.2 TPO run is shown in FIG. 1.

[0072] Table 2 compares the values of the T.sub.max of silver-zirconia catalysts with different Ag loading and calcination conditions. The 20Ag/ZrO.sub.2 catalyst exhibited improved activity when calcined at lower temperature (T.sub.max of 371° C. versus 377° C.). The activity of the 30Ag/ZrO.sub.2 catalyst remained unchanged within the range of experimental error.

TABLE-US-00002 TABLE 2 T.sub.max from TPO runs of Ag/ZrO.sub.2 catalysts calcined at different conditions T.sub.max (° C.) After calcination Catalyst 500° C. (10 h) 550° C. (6 h) 20Ag—ZrO.sub.2 371 377 30Ag—ZrO.sub.2 372 373

[0073] Further evaluation of Ag/ZrO.sub.2 catalysts calcined at different conditions was performed using a fixed-bed reactor with simulated diesel exhaust.

[0074] FIG. 2 depicts the carbon dioxide concentration versus temperature profiles for 20Ag/ZrO.sub.2 (calcined at 500° C., 10 h) and 30Ag/ZrO.sub.2 (calcined at 550° C., 6 h) tested with 10 vol % O.sub.2, 5 vol % H.sub.2O, 500 ppm NO in N.sub.2 and under tight contact mode.

[0075] The maximum rate of carbon combustion was observed at 335° C. (T.sub.max) for both catalysts.

[0076] This test demonstrated that the catalyst with the lower concentration of Ag exhibited the same activity for carbon oxidation as the catalyst with the higher Ag loading based on the same value of T.sub.max. The increased activity of 20Ag/ZrO.sub.2 catalyst may be due to the lower catalyst sintering during the calcination at milder conditions that resulted in the higher surface area of both zirconia and Ag active metal.

Engine Evaluation of Ag/ZrO.SUB.2 .Catalyzed Particulate Filter—BPT Determination

[0077] The catalyst performance for soot oxidation was initially evaluated by TPO in a flow reactor using simulated diesel exhaust conditions, carbon black as a model soot and tight contact between carbon and catalyst particles. These lab reactor studies revealed a high activity of the developed catalyst for elimination of soot particles in the temperature range typical of diesel exhaust (200-500° C.) and in the presence of oxygen, water and nitrogen oxide. However, due to lab testing limitations, engine evaluation was required in order to assess the catalyst activity under real engine exhaust conditions.

[0078] The regeneration performance of the Ag/ZrO.sub.2 catalyzed particulate filter loaded with the improved 20Ag/ZrO.sub.2 catalyst was evaluated during an engine test. The balance point temperature (BPT), at which combustion of soot occurs at the same rate as soot loading, was determined during this test and used as evaluation criteria of the filter regeneration degree. The determination of balance point temperature is a required step in the catalyzed particulate filter development.

[0079] A commercial CDPF (Cattrap, CDTi Advanced Materials Inc.) was tested at the same conditions for comparison. To determine the balance point temperature, the engine tests were conducted with no diesel oxidation catalyst (DOC) unit at the upstream of the filter.

[0080] The catalytic phase comprises the improved 20Ag/ZrO.sub.2 catalyst, which was loaded on the commercial 12.5 L wall-flow ceramic filter by slurry forcing method. After drying and calcination, the filter contained silver in the amount of 6.5 g/L.

[0081] FIG. 3 shows the schematic of a wall-flow Ag/ZrO.sub.2 catalyzed particulate filter 1.

[0082] The Ag/ZrO.sub.2 catalyzed particulate filter 1 has a porous monolithic ceramic substrate 2 formed of parallel channels 3 and composed of cordierite.

[0083] A catalyst layer 4 coats the walls of the ceramic substrate 2. Soot particles 5 are deposited on the walls of the channels as the exhaust gas passes through the filter.

[0084] In the inlet end, every other channel is plugged with ceramic material, while the adjacent channel is plugged at the outlet end 6. The wall-flow structure forces the exhaust gas 7 to pass through the porous channel walls enabling cleaner gases to exit 8.

[0085] Table 3 below shows specifications for the Ag/ZrO.sub.2 catalyzed particulate filter monolith.

TABLE-US-00003 TABLE 3 Catalyzed Particulate Filter Monolith Specifications Catalyzed Particulate Filter Part Number RDAB-01-5X57-21 Serial Number 296947 Core Model Duratrap AC Material Advanced Cordierite Diameter (mm) 230 Length (mm) 305 Geometric Vol (L) 12.7 Cell density (cpsi) 200 Wall thickness (mils) 12 Porosity (%) 50 Silver (non - platinum group 6.5 metal) loading (g/L)

[0086] The Ag/ZrO.sub.2 catalyzed particulate filter was tested with a Detroit Diesel heavy-duty engine (6063-WK32, Series 60, 11.1 L, 6 cylinder, Tier 1, turbocharger). The engine load was performed with an engine dynamometer.

[0087] The engine test bench setup shown in FIG. 4 consists of a Detroit Diesel engine 9 equipped with a Turbocharger 10 and a 12.5 L catalyzed particulate filter 11. The engine exhaust flow was split using splitter control valves 12 allowing a flow through the catalyzed particulate filter as high as possible, but that did not exceed 2 kPa delta pressure across the filter. The pressure drop, inlet and outlet temperatures of the catalyzed particulate filter were monitored by a differential pressure sensor and temperature thermocouples 13, 14.

[0088] A test procedure to determine the balance point temperature was developed based on a progressive load test in accordance with the program [Diesel Emissions Control Sulfur Effects (DECSE) Program, Phase 1, Interim Report 1, US Department of Energy, Washington D.C., August 1999]. The procedure involved preloading the filter with soot to a predetermined level. Then a stepwise increase of the filter's inlet temperature was undertaken by increasing the engine load that was accompanied by recording the filter pressure drop. The temperature at which the pressure drop decreased was determined as a filter balance point temperature.

[0089] Test Procedure: [0090] 1. Weighing clean catalyzed particulate filter before the soot loading phase, [0091] 2. Soot preloading at a preselected speed/load to a predetermined loading level, [0092] 3. Weighing catalyzed particulate filter after the soot loading phase, [0093] 4. Determination of the balance point temperature by increasing engine loads progressively, [0094] 5. Measuring catalyzed particulate filter inlet and outlet pressure and temperature for each load, [0095] 6. Determination of delta pressure from positive to zero and negative, in other words from the transition between filter loading and regeneration.

[0096] Testing results are presented on FIGS. 5 and 6.

[0097] FIG. 5 shows the pressure changes during engine testing of a catalyzed filter, wherein the catalyzed filter is an Ag/ZrO.sub.2 catalyzed particulate filter according to the present invention.

[0098] FIG. 6 shows the pressure changes during engine testing of a catalyzed filter wherein the filter is the same as used in commercial base metal-palladium “Cattrap” CDPF.

[0099] The balance point temperature was determined by analyzing the slope of the differential pressure for each temperature steps. The temperature of exhaust increased with load monotonically. The pressure drops across the filter increased with temperature initially and started to decrease at certain point. This point, at which the reduction in pressure drop was observed (in other words, when the rate of particles oxidation was approximately equal to the rate of particles loading), was defined as a balance point temperature.

[0100] According to testing results, both filters exhibited a capacity to burn diesel particulate matter. The balance point temperature for the Ag/ZrO.sub.2 catalyzed particulate filter (coated by the 20Ag/ZrO.sub.2 catalyst) was in the range 310 to 348° C., while the commercial base metal-palladium CDPF exhibited the balance point temperature in the range 378 to 450° C. matching closely the manufacturer's specifications.

[0101] The Ag/ZrO.sub.2 catalyzed particulate filter was found to have a significantly lower balance point than that of a commercially available base metal-palladium “Cattrap” CDPF as shown in Table 4 below.

TABLE-US-00004 TABLE 4 Balance Point Temperature of Two Tested Catalyzed Particulate Filters Balance point Balance point Type of filter temperature range (° C.) temperature (° C.) Ag/ZrO.sub.2 catalyzed 310-348 349 particulate filter “Cattrap” CDPF 378-450 454

[0102] Overall, the engine test results agreed with the lab test results confirming that the Ag/ZrO.sub.2 catalyzed particulate filter coated with a new less expensive silver-based catalyst (20Ag/ZrO.sub.2) offers low temperature oxidation of collected particulate matter, thus providing continuous passive regeneration of the filter at normal engine operating conditions.

[0103] A lowering of the balance point temperature allows avoiding active regeneration or decreasing the number of such cycles that reduce the use of fuel as well as CO.sub.2 emissions.

Emission Test

[0104] The impact of the developed CDPF on diesel emissions was examined on an engine dynamometer using a medium-duty Deutz F6L914 Tier 2 diesel engine approved for use in underground mines. Emission characteristics were obtained at progressive load test. This test cycle was run at eighteen (18) points from zero load to the maximum load at 1500 rpm. The diesel fuel was the same as used in the previous test. The experimental setup was the same as for the balance point temperature test using splitter and no DOC in front of the filter.

[0105] All engine basic conditions were monitored. The temperature of the CDPF was consecutively increased and at a given temperature the CDPF started to contribute to catalytically assisted chemical reactions. Gaseous emissions including carbon monoxide (CO), unburned total hydrocarbons (THC) and nitrogen oxides (NO.sub.x) were analyzed continuously at each points before (inlet port) and after (outlet port) the CDPF. The progressive load test was carried out on a “clean” CDPF, which had no preloaded PM. During the test, the pressure drop across the CDPF was also assessed.

[0106] The diesel PM was measured during the ISO 8178 C1 8-mode test cycle for non-road engine application. The 8-Mode test cycle for the Deutz F6L914 engine is defined in Table 5. Prior to the 8-Mode tests, the engine intake restriction at Mode 1 was adjusted to a maximum allowable value of 3 kPa for the engine, and similarly exhaust backpressure at Mode 1 was adjusted to a maximum allowable value of 10 kPa for all test cycles. The exhaust backpressure, CDPF inlet and outlet pressures, and exhaust temperature at the inlet and the outlet of the devices were recorded. PM was analyzed using a Sierra BG-3 partial flow dilution sampler.

TABLE-US-00005 TABLE 5 ISO 8178-C1 8-Mode test cycle Mode# 1 2 3 4 5 6 7 8 Engine Speed, rpm 2300 1500 600 Torque, % 100 75 50 10 100 75 50 0 Weighting factor 0.15 0.15 0.15 0.1 0.1 0.1 0.1 0.15

[0107] FIG. 7A shows that the CDPF inlet exhaust temperature was increased gradually by increasing the engine load in steps of about 20-25° C. The first two load points (20 to 40 N.Math.m), measured in the low range of the torque meter had a variance of ±30%; and as result the following discussion ignores these two points. During the test, the pressure drop across the CDPF was also assessed (FIG. 7B) and did not exceed 3.8 kPa.

Carbon Monoxide (CO)

[0108] FIG. 8A shows the variation of the CO concentration before and after the CDPF with the inlet CDPF temperature measured without pre-DOC. At low engine speed, the CO emissions were maximum in the range from 450 to 500 ppm at temperature 120° C. With the increase of the engine load, the CO concentration in the engine exhaust decreased continuously with the temperature raise. This is due to the improved engine performance at elevated temperature leading to the more efficient burning of the fuel.

[0109] The difference in CO concentrations between inlet and outlet ports was observed at temperatures higher than 350° C. (pointed by an arrow) due catalytic oxidation by the Ag-based catalyst coated the DPF.

[0110] At high load and the temperature of 450° C., the CO emissions has reached a minimum of ˜100 ppm that corresponded to the 35% improvement in CO reduction compared to its inlet concentration (FIG. 8B). An increase in CO concentration from 133 to 210 ppm was registered at the maximum engine load (480° C.) which was accompanied by the higher fuel/air ratio. As result, there was insufficient oxygen to convert fuel to carbon dioxide.

Unburned Total Hydrocarbons (THC)

[0111] FIG. 9A depicts the variation of the THC concentration with the inlet CDPF temperature measured without DOC in front of the filter, and it shows that THC emissions decreased with the increase of the load due to the more efficient combustion at elevated temperatures.

[0112] The Ag-based catalyst inside the CDPF started to oxidize THC at the temperature higher than 300° C. (pointed by an arrow) exhibiting the difference between inlet and outlet concentrations. From this point THC relative concentration permanently decreased (FIG. 9B). At the end of testing at 480° C., the final THC concentration after the CDPF was 76 ppm that was lower than that for the inlet port by 47%.

Nitrogen Oxides (NO and NO.SUB.2.)

[0113] NO and NO.sub.2 are formed due to incomplete fuel combustion and their content in diesel exhaust depends on engine parameters. One of these parameters is an in-cylinder temperature.

[0114] NO concentration versus the inlet temperature is shown in FIG. 10. The NO concentration varied linearly from 150 ppm up to the 715 ppm with engine load growth (120° C.-300° C.) that was in agreement with the influence of the combustion temperature on NO.sub.x formation. The overall impact of the CDPF on NO emissions was not pronounced since both inlet and outlet NO concentration curves are close. The minor difference between the inlet and outlet curves was found in a temperature range of 350 to 480° C. that may be due to the NO oxidation assisted by the catalyst.

[0115] FIG. 11A displays the variation in NO.sub.2 concentration for different loading conditions and without the DOC in front of the filter. In the temperature range from 120 to 480° C. the continuous decrease in the CDPF inlet NO.sub.2 concentration was observed because the thermodynamic equilibrium shifted towards NO and O.sub.2 at high temperatures. The outlet NO.sub.2 concentration changed differently. At relatively low temperatures (<300° C.) higher decrease of NO.sub.2 in outlet port may be due to its adsorption on the surface of the catalyst inside the CDPF forming mostly silver nitrates. NO.sub.2 adsorption was reflected in the relative decrease of NO.sub.2 concentration at this temperature range (FIG. 11B). The thermal decomposition of silver nitrates takes place at a temperature of 300-450° C. producing silver, NO.sub.2 and O.sub.2. Thus, a slight increase in NO.sub.2 concentration could be linked to the nitrate decomposition and desorption from the catalyst surface that corresponded to the positive values of the relative concentration change (FIG. 11B). While decomposition/desorption was getting lower (T>400° C.), the outlet concentrations became closer to the inlet ones exhibiting limited NO.sub.2 formation (24 ppm versus 15 ppm, respectively). Overall, the catalyst coat did not produce significant amount of extra NO.sub.2 at all exhaust temperatures.

Emissions 8-Mode Test

[0116] FIG. 12 shows the comparison of PM emissions measured at inlet and outlet of the CDPF during 8-mode emission test.

[0117] As the inlet temperature increased (mode 1 and 5), the PM emissions increased and reached the highest values of 8.7 g/hr. The efficiency of the PM reduction for these modes corresponded to 85 and 95%, respectively. The mode 8 with the lowest load and temperature showed the lowest value of 1.6 g/hr PM in the exhaust and efficiency of the PM reduction of 93%. In the middle range of operating temperatures the PM emissions varied between 2 and 4 g/hr and the PM reduction changed from 68 (mode 3) to 86% (mode 7). Overall, the average reduction of PM mass through the CDPF was found to be 85.7% (Table 6), which would meet the EPA Tier 4 requirements of 0.02 g/kW.

[0118] A summary of other emissions assessment is presented in Table 6. The average percentage of emission change was calculated from the 8-mode test. At average temperature of 325° C., a significant reduction in THC and approximately 37% was observed demonstrating catalyst activity for hydrocarbon oxidation under experimental conditions.

[0119] Additionally, Table 6 shows the decrease of CO emissions by approximately 15% that was due to the oxidation of CO by the catalyst. NO.sub.2 emissions were decreased in average by 30%, however, total amount of NO.sub.x did not change significantly due to the back reduction of NO.sub.2 to NO during soot oxidation. Overall, the impact of the developed aftertreatment device did not significantly affect NO.sub.x emissions removal.

TABLE-US-00006 TABLE 6 Integrated 8-Mode Emissions Weighted Weighted Emission Average Average Change Test Points Units (Inlet) (Outlet) (%) Parameters Speed rpm 1845 1845 .sup. NA.sup.a Torque N .Math. m 174.9 175 NA Power kW 35.4 35 NA Exhaust temperature ° C. 344.8 343.3 −0.4 CDPF temperature ° C. 325.9 323.4 −0.8 Emissions CO.sub.2 g/hr 28685 28583 −0.4 CO g/hr 99 84 −15.2 NO.sub.2 g/hr 24 17 −29.2 NO g/hr 192 195 1.6 NO.sub.x g/hr 215 212 −1.4 THC g/hr 38 24 −36.8 PM g/hr 4.06 0.58 −85.7 g/kWt 0.110 0.016 .sup.aNot applicable

[0120] The present invention discloses that the developed CPDF is effective for the passive regeneration at temperatures from 300° C. with a BPT of 350° C. that is 100° C. lower than that of the commercial filter indicating the better performance of the new catalytic Ag-based coating compared to that of the commercial base metal-palladium Cattrap filter.

[0121] A lowering of the BPT allows avoiding active regeneration or decreasing the number of such cycles that lower fuel penalty and related CO.sub.2 emissions.

[0122] The average reduction of CO, THC and NO.sub.2 obtained during emission test with the novel CDPF were found to be 15%, 37% and 30%, respectively, within a wide temperature range. Furthermore, the average effectiveness of the PM mass removal was found to be higher than 85% keeping the back pressure within the application requirements for the engine. The advantage of using Ag-based catalyst is the elimination of NO.sub.2 slip from the CDPF that could avoid increasing the ventilation airflow rates.

[0123] The tested Ag-based catalyst coated CDPF presents advantages economically due to the lower cost of silver compared to that of palladium, but still possessing sufficient ability to oxidize PM, CO and THC.

[0124] Therefore, the developed CDPF presents a suitable and less expensive alternative to the base metal-palladium commercial filter for PM removal.

[0125] While the present invention has been described in considerable detail with reference to certain preferred and/or exemplary embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the present invention without departing from the essential scope thereof. Therefore, the scope of the appended claims should not be limited by the preferred embodiments set forth in the examples, but should be given the broadest interpretation consistent with the description as a whole.