FIELD OF THE INVENTION

The present invention relates to a process for preparation of mixed metal oxide based diesel oxidation catalyst (DOC) for complete oxidation of hydrocarbons and carbon monoxide from diesel engine exhaust. The catalyst is non-noble metal based.

BACKGROUND OF THE INVENTION

The diesel engine based vehicles have become more popular for both passenger cars as well as for heavy vehicles for transportation and other applications. However, it is well known fact that these engines emit large amount of hydrocarbons (HCs), carbon monoxide, NOx and particulate matter (PM) due to incomplete combustion of fuel and other processes at higher temperature in internal combustion diesel engines. Due to the concern about the environmental pollution and stringent emission regulations, there is a need to control the emission of these pollutants like NO _x , CO and unbumt hydrocarbons (HCs). Oxidation catalysts have been used to oxidize CO, HC and NOx to clean up the diesel engine exhaust. Noble metal based catalysts, particularly Pt and Pd supported on alumina have been used as DOC for oxidation of hydrocarbon and CO to C0 ₂ as well as oxidation of NOx to N0 ₂ which is used for the oxidation of particulate matter. Sometimes, the diesel engine exhaust contains large quantity of S0 ₂ due to the higher sulfur content in the diesel fuel, because of which the noble metal based catalysts gets deactivated due to sulfur poisoning. The diesel engine exhaust temperature sometimes exceeds >600 °C, particularly for heavy vehicle diesel engine, and then in the Pt, Pd based catalysts where the Pt, Pd, are dispersed on high alumina support, get agglomerated /sintered thus lowering the catalytic activity of the diesel oxidation catalysts.

I WO 2009/074308 or EP 2070581 Al relates to a catalyst containing a carrier and a coating, characterized in that the coating comprises a support material and at least one zeolite, the support material comprising platinum, palladium and at least one promoter selected from the group consisting of Mg, Ca, La, Ti, Zr, Hf, Au, Si, Sn, P compounds or mixtures of these promoters, loaded thereon. The document also relates to a process for the manufacture of the catalyst and the use thereof for the purification of exhaust gases from Diesel and lean Otto engines. The catalyst effectively oxidizes carbon monoxide and hydrocarbons, has a high resistance towards hydrothermal aging and is stable during operation.

EP1925362, US2008/0124514, US7,517,826 and US7,534,738 disclose diesel oxidation catalysts in which there is a mixture of a first and a second catalytically active material. For production of the first catalytically active material, palladium in addition to gold is supported on a lanthanum oxide-stabilized aluminum oxide. As the second catalytically active material, platinum is applied, optionally together with palladium or bismuth, to lanthanum oxide-stabilized aluminum oxide. The two catalytically active materials may be applied to an inert honeycomb as a homogeneous powder mixture in E catalytically active layer or in the form of a plurality of different coatings (for example as a Zone catalyst or layer catalyst). In the case of multilayer catalysts, it is additionally possible for Zeolite containing intermediate layers and/or layers comprising palladium supported on cerium oxide to be present.

WO 2009/ 106849 and US20110113774 disclose diesel oxidation catalysts whose features include high conversion rates for methane and presence of palladium and gold as active components, preferably in alloyed form. For preparation of the catalysts, palladium ex palladium nitrate and gold ex tetrachloroauric acid are applied by precipitation and calcination to aluminum oxide as the support material. The powder component thus obtained can be used to prepare a suspension for coating of conventional flow honeycombs as the catalyst substrate. WO 2008/1 17941 discloses diesel oxidation catalysts which feature improved HC oxidation activity and comprise palladium alloyed with gold on aluminum oxide as the first catalytically active material, in addition to platinum alloyed with palladium on aluminum oxide as the second catalytically active material. Instead of aluminum oxide, it is also possible to use other inorganic support oxides, for example silicon dioxide, aluminum silicate, silicates, titanium oxide, Zirconium oxide, SiC and carbon black. A diesel oxidation catalyst produced from the mixture of the catalytically active materials may further comprise oxygen-storing rare earth metal oxides.

US 2008/125308 describe exhaust gas catalysts which comprises a platinum-containing catalyst and a palladium- and gold-containing catalyst, which may additionally comprise Zeolite as an absorbent for hydrocarbons. The two catalysts are arranged in various catalytically active Zones of the exhaust gas catalyst, in such a way that the exhaust gas encounters the platinum catalyst first. This is achieved by means of customary layer or zone arrangement of the two catalysts, or by virtue of the two catalysts being supported on different monoliths.

Article titled, "Cooperative effect of Ce and Mn in MnCe/Al203 environmental catalysts" by Hadjiivanov et al. in Appl Catal. B: Env. 2013, 138- 139, 362- 372 reports a series of alumina supported catalysts containing Ce and Mn with different ratios for methanol decomposition or NO reduction with methanol decomposition products.

US 6,274,107 discloses an oxidation catalyst, which contains cerium oxide, optionally aluminum oxide and a zeolite, for example zeolite beta. The zeolite can be doped with the metals of the platinum group and other metals or metal species, such as Pt, h, Pd, Ru, Os, Ir, Cu, Fe, Ni, Cr, and V. The catalyst promotes the oxidation of CO, HC. EP 0432534B2 and US 20080279738 disclose a continuously working oxidation catalyst having high conversion performance for hydrocarbons and carbon monoxide in low temperature ranges. The catalyst consists of vanadium compounds and metals of the platinum group, which are applied on aluminum oxide, titanium oxide, silicon oxide, zeolite as well as mixtures thereof. According to Tables 2 and 3 of these documents, the values for the 50 % conversion of CO and HC (T ₅₀ values which are also termed as light-off temperature) for the freshly prepared catalysts are above 200 °C.

US 7,078,004 discloses a method for treating diesel exhaust gas stream whereby the stream is contacted with an upstream catalyst comprising a cerium component and/or a zeolite component and a particulate filter located downstream from the upstream catalyst. The framework alumina of the zeolite component can be substituted by at least one metal selected from the group B, Ga, In, Fe, Cr, V, As. The exchangeable cationic component of the zeolite can be selected from the group consisting of hydrogen and at least one metal selected from the group consisting of Li _\ Na, K, Rb, Cs, Mg, Caj Sr, Bai Cr, Mm Fe, Co, Ni, Cu, Nb, Ma, Ta, W, Re, Pt, Pd and Rh.

US 6093378 discloses a catalyst composition and structure containing the same and methods for treating diesel exhaust including a catalyst comprising a precious metal on a support, a first zeolite component in the presence of a precious metal and a second zeolite component comprising a zeolite and a precious metal, and a non-catalytic pore- containing zeolite.

US 2013/0202509 relates to a catalytically active material consisting of an inner core (1) and an outer shell (2) surrounding this core, the core being formed from palladium and gold fixed together on a first support oxide, and the shell comprising platinum fixed on a second support oxide, to a diesel oxidation catalyst comprising this catalytically active material, and to an exhaust gas cleaning system comprising this diesel oxidation catalyst.

US 2011/0044871 relates to a coating composition for diesel oxidation catalysts or a combination of diesel oxidation catalysts and diesel particle filters, said coating composition comprising a combination of a noble metal on a metal oxide, with the exception of cerium oxide, and a zeolite doped with iron. The invention also relates to a catalyst provided with the coating and to a method for treating the exhaust gas of diesel internal combustion engines. US5,491 ,120 discloses oxidation catalysts containing ceria and a bulk second metal oxide which may be one or more of titania, Zirconia, ceria-Zirconia, silica, alumina silica and alpha-alumina.

Considering the higher cost of noble metal based catalysts and its deactivation due to sulfur poisoning or sintering effects, development of a non noble metal based catalyst for oxidation of hydrocarbons and CO is highly desired.

OBJECTIVES OF THE INVENTION

An object of the present invention is to provide a non noble metal based diesel oxidation catalyst.

Another objective of the present invention is to provide a process for the synthesis of the non-noble metal based diesel oxidation catalyst.

Yet another objective of the present invention is to provide a non noble metal based catalysts for oxidation of hydrocarbon and carbon monooxide (CO) at low temperature. Yet another objective of the present invention is to provide a non-noble metal based catalyst with sulfur tolerance and water resistance.

SUMMARY OF THE INVENTION

Accordingly, the present invention provides a diesel oxidation catalyst comprising a mixed oxide of A and B, wherein A is Mn and B is Ce or a mixture of Ce and Zr, said catalyst comprises A in the range of 1- 60% by weight of the catalyst and B in the range of 40-99% by weight of the catalyst, wherein the catalyst is devoid of noble-metal and is having Mn particle size of 50-70 % particles < lnm; said catalyst is prepared by a process comprising: a) mixing salt of A and salt of B in water or a mixture of water and an acid to obtain a solution; b) adjusting pH of the solution obtained in step (a) in the range of 7-12; c) heat treating the solution of (b) to a temperature in the range of 100-200 °C for 15-120 minutes to obtain a reaction mixture; d) cooling and filtering the reaction mixture to obtain a residue; and e) washing and calcinating the residue obtained in step (d) at a temperature in the range of 300-800 °C for 1-5 hours to obtain the diesel oxidation catalyst.

In one embodiment of the invention the BET surface area of the catalysts is 100-160 m /g with a pore volume of 0.200 to 0.381 cm /g. In an embodiment of the invention the salt of A and B is selected from the group consisting of nitrate, acetate.

In another embodiment of the invention the acid used is nitric acid.

In another embodiment of the invention the catalyst according to claim 1 is useful in oxidation of hydrocarbons and carbon monoxide from diesel engine exhaust. Still in another embodiment of the invention the catalyst oxidizes carbon monoxide (50 % conversion) at a temperature in the range of 30 to 250 °C.

Still in another embodiment of the invention the catalyst exhibits sulphur tolerance with oxidation of carbon monooxide (50% conversion) at a temperature in the range of 200 to 300 °C. Still in another embodiment of the invention the catalyst exhibits water tolerance with oxidation of carbon monooxide (50% conversion) at a temperature in the range of 220 to 300 °C.

BRIEF DESCRIPTION OF THE DRAWINGS: Fig. 1 : TEM images of catalyst prepared in Example 3. Fig. 2: depicts the diesel (propene) oxidation activity of the catalysts in comparison to Pt catalyst.

Fig. 3: depicts diesel oxidation (propene) activity at 50000 h ^"1 GHSV

Fig. 4: Diesel oxidation (propene) activity at 100000 h ^"1 GHSV

Fig. 5: Water tolerance of catalyst prepared in Example 3 (propene)

Fig. 6: Sulfur tolerance of catalyst prepared in Example 3.

Fig. 7: Oxidation activity (Propene + CO) of the catalyst prepared in Example 3

Fig. 8: Depicts the (CO) diesel oxidation activity of the catalysts in comparison to Pt catalyst.

Fig. 9: Diesel oxidation activity (Propene) of catalyst prepared in Example 5 Fig. 10: Sulfur tolerance (Propene) of catalyst prepared in Example 5.

Fig. 11 : Water tolerance of (Propene) catalyst prepared in Example 5.

Fig. 12: Diesel oxidation activity (CO) of catalyst prepared in Example 5

Fig. 13: Sulfur tolerance of catalyst (CO) prepared in Example 5.

Fig. 14: Water tolerance of catalyst (CO) prepared in Example 5.

Fig. 15: Diesel oxidation activity (CO) of catalyst prepared in Example 6

Fig. 16: Diesel oxidation activity (CO) of catalyst prepared in Example 7

DETAILED DESCRIPTION OF THE INVENTION:

The invention will now be described in detail in connection with certain preferred and optional embodiments, so that various aspects thereof may be more fully understood and appreciated.

The present invention provides a diesel oxidation catalyst comprising a mixed oxide of A and B, wherein A is Mn and B is Ce or a mixture of Ce and Zr, said catalyst comprises A in the range of 1-60% by weight of the catalyst and B in the range of 40- 99% by weight of the catalyst, wherein the catalyst is devoid of noble-metal and is having Mn particle size of 50-70 % particles < lnm; said catalyst is prepared by a process comprising:

a) mixing salt of A and salt of B in water or a mixture of water and an acid to obtain a solution;

b) adjusting pH of the solution obtained in step (a) in the range of 7-12;

c) heat treating the solution of (b) to a temperature in the range of 100-200 °C for 15-120 minutes to obtain a reaction mixture;

d) cooling and filtering the reaction mixture to obtain a residue; and

e) washing and calcining the residue obtained in step (d) at a temperature in the range of 300-800 °C for 1-5 hours to obtain the diesel oxidation catalyst.

The diesel oxidation catalyst is prepared by modified co-precipitation method and hydrothermal treatment with different molar ratios of salts of A and B.

The BET surface area of the diesel oxidation catalysts is >150 m ² /g with a pore volume of 0.381 cm ³ /g for Mn ₀ . ₅ Ce ₀ .5O ₂ .

The catalyst was tested for diesel oxidation using propene, carbon monoxide as model compounds of diesel exhaust and sulphur tolerance and its activity was compared with 1 wt% Pt/Al ₂ 0 ₃ as reference catalyst.

In another embodiment of the present invention, the catalyst oxidizes carbon monoxide (50% conversion) at temperature in the range of 30 to 250 °C.

The diesel oxidation of the catalyst is studied by estimating propene and CO oxidation in a quartz tubular reactor. The detailed protocol is provided in example 9. In another aspect, the Mn-Ce catalyst shows lower light off temperature compared to Pt/Al ₂ 0 ₃ and shows 100% conversion at 200 °C for propene and 120°C for CO which is comparable with that of Pt/Al ₂ 0 ₃ .

With reference to Fig: 2, diesel oxidation activity of the catalyst prepared in Example 3 shows 100% propene conversion at 300 °C in presence of water, exhibiting the water tolerance of the catalyst of the present invention.

The present invention, the diesel oxidation activity of catalyst shoes 100% propene conversion at 200 to 300 °C in presence of S0 ₂ , referring to Fig: 6.

The present invention, the oxidation activity of catalyst shows 100% propene conversion at 220 to 300 °C at higher gas velocities (50000 h ^"1 ), referring to Fig: 7.

EXAMPLE

The following examples are given by way of illustration of the working if the invention is actual practice and shall not be construed to limit the scope of the present invention in anyway.

Example 1

Ce(N0 ₃ ) ₃ :6H ₂ 0 (12.623 g) and 0.798 g of Mn(OAc) ₂ :4H ₂ 0 were dissolved in 80 mL deionized water. To this solution, NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10 was obtained. The mixture was stirred additionally for 24 h at room temperature. The mixture was then transferred to 300 mL teflon-lined stainless steel autoclave and kept static at 120 °C for 40 min and cooled to room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for 12 h. Then it was calcined at 500 °C for 5 h at the rate of 2 °C min Example 2

Ce(N0 ₃ ) ₃ :6H ₂ 0 (12.623 g) and 3.054 g of Mn(OAc) ₂ : 4H ₂ 0 were dissolved in 80 mL deionized water. To this solution, NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10 was obtained. The mixture was stirred for additionally 24 h at room temperature. The mixture was transferred to 300 mL teflon- lined stainless steel autoclave and kept static at 120 °C for 40 min and cooled to room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for 12 h. Then it was calcined at 500 °C for 5 h at the rate of 2 °C min ^"1 .

Example 3

12.623 g Ce(N0 ₃ ) ₃ : 6H ₂ 0 and 7.126 g of Mn(OAc) ₂ : 4H ₂ 0 was dissolved in 80 mL deionized water. To this solution NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10. The mixture was stirred for additionally 24 h at room temperature. The mixture was transferred to 300 mL teflon- lined stainless steel autoclave and kept static at 120 °C for 40 min and cooled to room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for 12 h. Then it was calcined at 500 °C for 5 h at the rate of 2 °C min ^"1 .

Example 4

The catalyst prepared in Example 3 was characterized by HR-TEM using Tecnai FEI G2 microscope, using an accelerating voltage of 300 kV. For TEM analysis, a sample was dispersed in isopropanol by an ultrasonic bath and deposited on a coated 200 mesh Cu grid. The results are shown in Figure 1. The TEM analysis showed that majority of manganese particles (50-70%) are < 1 nm size. Example 5

Ce(N0 ₃ ) ₃ :6H 0 (30.563 g), Zr(N0 ₃ ):6H ₂ 0 (7.957g) and Mn(OAc) ₂ :4H ₂ 0 (9.970) was dissolved in 300 mL deionized water and 14 mL cone. HN0 ₃ acid. To this NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10. The mixture was stirred additionally for 24 h at room temperature. The mixture was transferred to 300 mL teflon-lined stainless steel autoclave and kept at 120 °C for 40 min and cooled to room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for overnight. Then it was calcined at 500 °C for 5 h at the rate of 2 °C min ^"1 .

Example 6

Ce( 0 ₃ ) ₃ :6H ₂ 0 (20.156 g), Zr(N0 ₃ ):6H ₂ 0 (5.297 g) and Mn(OAc) ₂ :4H ₂ 0 (6.571 g) was dissolved in 120 mL deionized water and 5 mL Cone. HN0 ₃ acid. To this solution NH ₃ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10. The mixture was stirred additionally for 24 h at room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for overnight. Then precipitate was calcined at 500 °C for 5 h at the rate of 2 °C min ^"1 .

Example 7

Ce(N0 ₃ ) ₃ :6H ₂ 0 (10.193 g), Zr(N0 ₃ ):6H ₂ 0 (2.676 g) was dissolved in 120 mL deionized water and 7 mL Cone. H O3 acid. To this solution NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10. The mixture was stirred additionally for 24 h at room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature and followed by drying at 80 °C for overnight. Then precipitate was calcined at 500 °C for 5 h at the rate of 2 °C min ^"1 . To this calcined material 200 ml deionised water was added to form slurry. To this slurry Mn(OAc) ₂ :4H ₂ 0 (5.329 g) in 30 mL deionized water was added. To this solution NH ₄ OH (10% v/v in water) solution was added dropwise with constant stirring till pH 10. The mixture was stirred additionally for 24 h at room temperature. The final reaction mixture was filtered and washed with water. The final residue was dried at room temperature followed by drying at 80 °C for overnight. Then precipitate was calcined at 500 °C for 5 h at the rate of 2 °C min

Example 8

The manganese content in the catalyst was estimated by ICP-AES using Spectra Arcos instrument. ~ 20 mg sample was dissolved in 10 mL aqua regia by an ultrasonic bath and diluted to 100 mL after digestion on hot plate at 80 °C. The results are shown below:

Example 9

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. The catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10%) 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ , and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desired gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41). The activity was compared with 1% Pt/Al ₂ 0 ₃ (commercial composition prepared in house by impregnating aqueous solution of platinum chloride on γ-Αΐ ₂ 0 ₃ ) under identical reaction conditions and the results are given in Figure 2. The figure shows that the (propene) oxidation activity of catalyst prepared in example 3 is comparable with Pt/Al203 with better low temperature activity compared to Pt/A1203 and almost comparable temperature for 100% propene conversion.

Example 10

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60- 120 mesh (2 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ , and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desired gas hourly space velocity of 50,000 h ^" \ The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41). The results of the activity are given in Figure 3. Diesel oxidation activity of catalyst prepared in example 3 showed 100% propene conversion at 230 °C. Example 11

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60- 120 mesh (2 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% Oi in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ , and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desired gas hourly space velocity of 1,00000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41). The results of the activity are given in Figure 4. Diesel oxidation activity of catalyst prepared in Example 3 showed 100% propene conversion at 250 °C.

Example 12

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ + 9% H ₂ 0 and He gas as a balance. Water was supplied to the reactor by peristaltic pump (Tris ISCO) through a preheated evaporator to generate steam. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5 A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41), 0 ₂ (32). The results of the activity are given in Figure 5. Diesel oxidation activity of catalyst prepared in example 3 showed 100% propene conversion at 300 °C in presence of water.

Example 13

The diesel oxidation activity of the prepared catalyst in Example 3 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ + 10 ppm S0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29), C ₃ H ₆ (41). The results of the activity are given in Figure 6. Diesel oxidation activity of catalyst prepared in Example 3 showed 100% propene conversion at 250 °C in presence of S0 ₂ .

Example 14

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially, thecatalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 300 ppm CO + 10% 0 ₂ + 10% C0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41), 0 ₂ (32). The results of the activity are given in Figure 7. Oxidation activity of catalyst prepared in Example 3 showed 100% propene conversion at 220 °C and 100% CO conversion at 205 °C

Example 15

The diesel oxidation activity of the catalyst prepared in Example 3 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ , and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desired gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29). The results of the activity are given in Figure 8. Oxidation activity of catalyst prepared in Example 3 showed 100% CO conversion at 125 °C

Example 16 The diesel oxidation activity of the catalyst prepared in Example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 25 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ , and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desired gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for C0 ₂ (44), CO (29), C ₃ H ₆ (41). The results of the activity are given in Figure 9. Diesel oxidation activity of catalyst prepared in Example 5 showed 100% propene conversion at 195 °C.

Example 17

The diesel oxidation activity of the catalyst prepared in Example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ + 10 ppm S0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29), S0 ₂ (64), C ₃ H ₆ (41). Diesel oxidation activity of catalyst prepared in example 5 showed 100% propene conversion at 200 °C in presence of S0 ₂ . The results of the activity are given in Figure 10. Diesel oxidation activity of catalyst prepared in example 5 showed 100% propene conversion at 200 °C in presence of S0 ₂ .

Example 18

The diesel oxidation activity of the catalyst prepared in Example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 300 ppm propene + 5% 0 ₂ + 9% H ₂ 0 and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29), C ₃ H ₆ (41). The results of the activity are given in Figure 11. Diesel oxidation activity of catalyst prepared in example 5 showed 100% propene conversion at 325 °C in presence of H ₂ 0.

Example 19

The diesel oxidation activity of the catalyst prepared in Example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29). The results of the activity are given in Figure 12. Diesel oxidation activity of catalyst prepared in example 5 showed 100% CO conversion at 145 °C.

Example 20

The diesel oxidation activity of the catalyst prepared in Example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ + 10 ppm S0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29), S0 ₂ (64). The results of the activity are given in Figure 13. Diesel oxidation activity of catalyst prepared in example 5 showed 100% CO conversion at 165 °C in presence of S0 ₂ .

Example 21

The diesel oxidation activity of the catalyst prepared in example 5 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ + 9% H ₂ 0 and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29). The results of the activity are given in Figure 14. Diesel oxidation activity of catalyst prepared in example 5 showed 100% CO conversion at 200 °C in presence of H ₂ 0.

Example 22

The diesel oxidation activity of the catalyst prepared in Example 6 was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^"1 . The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29). The results of the activity are given in Figure 15. Diesel oxidation activity of catalyst prepared in example 6 showed 100% CO conversion at 235 °C. Example 23

The diesel oxidation activity of the catalyst in example 7 catalyst was tested in down flow reactor. Typically reaction was carried out in a quartz tubular reactor (inner diameter 4 mm) at atmospheric pressure. Catalyst (0.5 g) was diluted with commercial silica gel of 60-120 mesh (2.0 g) and loaded in the quartz reactor. The reactor was heated with the help of electrically heated furnace. Initially catalyst was heated at 500 °C for 1 h in flow of 10% 0 ₂ in He and then reactor was cooled to 50 °C. The reaction was carried out by passing 1000 ppm CO + 5% 0 ₂ and He gas as a balance. The total flow of the gases was controlled by mass flow controllers to get desire gas hourly space velocity of 20,000 h ^~ \ The concentrations of the inlet and outlet gases were simultaneously monitored using Micro GC (Agilent 3000 A), fitted with molecular sieves to detect different gases (MS 5A, for 0 ₂ , CO), quadrupole mass spectrometer (Hiden, HPR 20) for 0 ₂ (32) C0 ₂ (44), CO (29). The results of the activity are given in Figure 16. Diesel oxidation activity of catalyst prepared in example 7 showed 100% propene conversion at 200 °C.

Advantages of invention:

• Non noble- metal based catalyst

Easy method of preparation

• Oxidation activity comparable with that of Pt/Al ₂ 0 ₃ .

Lower light off temperature compared to Pt/Al ₂ 0 ₃ • Expected cost will be much cheaper compared to commercial Pt based catalyst

(USD 2.2/Kg for Mn).

Catalyst shows good sulphur tolerance

Catalyst shows good water tolerance