PROCESS AND APPARATUS FOR REDUCING THE NITROGEN OXIDE CONTENT IN EXHAUST GASES BY THE CONTROLLED ADDITION OF NH3

Abstract: In the reduction of quantities of Nox in the exhaust gases of lean burn engines such as diesel engines, using a selective reduction catalyst and a source of ammonia, the present invention improves overall conversion by supplying ammonia or a precursor intermittently so that it is adsorbed and desorbed during the engine operating cycle.

Description: PROCESS AND APPARATUS FOR REDUCING THE NITROGEN OXIDE CONTENT IN EXHAUST GASES BY THE CONTROLLED ADDITION OF NH3 This invention concerns combatting air pollution from the exhaust gas of a lean burn engine. In particular, it concerns apparatus for, and a method of, reducing the content of nitrogen oxides (NOx) in such gas. Lean burn engines (which have an air-fuel ratio greater than 14.7, generally in the range 19-50) exhibit higher fuel economy and lower hydrocarbon emissions than do stoichiometrically operated engines and are increasing in number. Emissions from diesel engines are now being regulated by legislation, and whilst it is not too difficult to meet regulations on hydrocarbon or CO emissions, it is difficult to meet regulations on NOx emissions. Since exhaust gas from lean burn engines such as diesel engines is high in oxygen content throughout the engine cycle, it is more difficult to reduce NOx to nitrogen than in the case of stoichiometrically operated engines. The difficulty is compounded by the lower gas temperature. Various approaches are being considered to reduce NOx under the oxidising conditions. One approach is that of selective catalytic reduction (SCR) with hydrocarbon, but a catalyst of sufficient activity and durability to achieve the required conversion has not been found. Another approach is to adsorb the NOx by an adsorbent when the exhaust gas is lean (ie when there is a stoichiometric excess of oxygen) and release and reduce the adsorbed NOx when the exhaust gas is rich, the exhaust gas being made rich periodically. During the lean operation, NO is oxidised to N0 2 which can then react readily with the adsorbent surface to form nitrate. This approach, though, is constrained at low temperature by restricted ability to form NO 2 and by adsorbent regeneration and at high temperature by sulphur poisoning. Most adsorbents operate in a certain temperature window and are deactivated by sulphate formation. The approach of the present invention is that of SCR of NOx by NH 3 . This approach has been applied to static diesel engines using a V 2 O 5 - TiO 2 type catalyst. The application of NH 3 SCR technology to the control of NOx emission from lean burn vehicles, however, requires a suitable NH 3 supply strategy, especially at low temperature, for various reasons. The engine-out NOx varies with temperature, so the amount of NH 3 supplied must be well controlled as a function of the temperature to maintain the appropriate stoichiometry for the reaction; an insufficient supply of NH 3 results in inadequate NOx reduction, whilst an excess may cause NH 3 to slip past the catalyst. Whilst at sufficiently high temperature, the catalyst can selectively oxidise that excess NH 3 to N 2 , at low temperature, the unreacted NH 3 will be emitted as such. Even if the proper stoichiometry of NH 3 is provided, the catalyst may not be sufficiently active at low temperature to react all the NH 3 with the NOx. For example, Figure 1 shows the reaction of NH 3 with NOx over a non-metallised zeolite as a function of temperature at a stoichiometry of 1 : 1 at an inlet concentration of 200ppm. It can be seen that at temperatures below 300°C the reduction does not proceed to any significant extent. Furthermore, it has been reported that the presence of excess NH 3 at low temperature could lead to the formation of NH 4 NO 3 and (NH 4 ) 2 SO 4 . There is also evidence that the presence of excess gas phase NH 3 can inhibit the NH 3 SCR reaction over some catalysts at low temperature. Urea is usually the preferred form of storing NH 3 on a vehicle. Urea is readily available and is stable in water solution. However, it only hydrolyses readily to NH 3 at temperatures greater than 150°C, and may not be a suitable source of NH 3 at low temperature. Exhaust gas temperatures, though, vary over an engine cycle and for the average light duty diesel car a significant fraction of that cycle is at low temperature. Thus, the control of NOx at low temperature is a problem. The present invention provides an improved apparatus and method for reducing the content of NOx. Accordingly, the invention provides apparatus for reducing the content of nitrogen oxides (NOx) in the exhaust gas of a lean burn engine, which apparatus comprises: (a) exhaust apparatus through which the exhaust gas flows; (b) selective catalytic reduction catalyst in the exhaust apparatus, the catalyst catalysing the reduction of the NOx by ammonia to nitrogen and adsorbing and desorbing ammonia during the engine cycle; (c) a source of the ammonia; (d) supply means to supply the ammonia from the source to the catalyst; and (e) means to make the supply of ammonia intermittent during the engine cycle; whereby the catalyst adsorbs ammonia during its supply and the ammonia which has been adsorbed reacts with the NOx when the ammonia is not supplied. The invention provides also a method of reducing the content of nitrogen oxides (NOx) in the exhaust gas of a lean bum engine, which method comprises passing the exhaust gas over a selective catalytic reduction catalyst which catalyses the reduction of the NOx by ammonia to nitrogen and which adsorbs and desorbs ammonia during the engine cycle, ammonia being supplied intermittently to the catalyst during the engine cycle, the catalyst adsorbing ammonia during its supply and the ammonia which has been adsorbed reacting with the NOx when the ammonia is not supplied. We have discovered that ammonia can be adsorbed on a SCR catalyst and thereafter used in the NOx reduction when ammonia is not being supplied. It is an advantage to be able to achieve the NOx reduction while supplying the ammonia intermittently. In particular, the ammonia supply can be halted and yet NOx reduction occur when the temperature of the catalyst is low and supply would have the problems referred to above. The stored ammonia can be used as reductant for NOx over the same catalyst without the presence of gas phase NH 3 . The ammonia can be supplied without the exhaust gas so that the catalyst adsorbs the ammonia and then the exhaust gas passed over the catalyst for the NOx reduction to occur Preferably, however, the exhaust gas is passed continuously over the catalyst. The invention uses adsorption and desorption characteristics of the required catalyst. A higher amount of NH 3 will be adsorbed, and hence be available for subsequent reaction, if adsorption is at a lower temperature than temperatures at which the catalyst adsorbs less NH 3 . Preferably NH 3 is adsorbed at a temperature at which a large amount is adsorbed; the temperature is preferably below that of maximum desorption. The temperature, however, is preferably above that at which any significant formation of ammonium salts occurs. Figure 2 shows the desorption profile from zeolite ZSM5 (non-metallised) of NH 3 which had been pre-adsorbed at 100° C. It can be seen that at say 300°C more NH 3 is retained, adsorbed, than at say 400 °C, and that the temperature of maximum desorption is about 370 °C. Bearing in mind that the desorption of NH 3 is endothermic, it can also be seen that if NH 3 were adsorbed at say 300 °C and then heated, NH 3 would be desorbed in accordance with the graph so that less would be available for subsequent reaction, while if NH 3 were adsorbed at the same temperature, 300°C, and cooled, NH 3 would not be desorbed so the adsorbed NH 3 would be available for subsequent reaction. NH 3 stored on the ZSM5 catalyst at 250 °C can effectively be used to reduce NOx at a temperature as low as 150°C under exhaust conditions simulating those of a light duty diesel car. Figure 3 shows the NH 3 uptake of ZSM5 catalyst (non-metallised) from a gas mixture containing 4.5% C0 2 , 12% O 2 , 4.5% H 2 O, 200ppm CO, 1 OOppm C 3 H 6 , 20ppm SO 2 and 200ppm NH 3 with the balance N 2 at 250°C, and Figure 4 shows the subsequent reaction of that adsorbed NH 3 with NOx at 150°C. It can be seen that significant amounts of NOx are reduced by the adsorbed NH 3 over a period of time and that as the stored NH 3 is being consumed, the reduction reaction declines with time. When the temperature rises in the engine cycle, however, NH 3 can be supplied again, and hence adsorbed NH 3 replenished. Accordingly, the problem of supplying NH 3 at low temperature can be overcome by halting its supply and using adsorbed NH 3 . The amount of NH 3 adsorbed on a fixed weight of catalyst can be increased by increasing its partial pressure in the gas mixture. For example, Table 1 gives the amount of NH 3 adsorbed by a zeolite at 250 °C from a simulated gas mixture of differing NH 3 concentrations. TABLE 1 NH 3 Adsorption as a Function of NH 3 Concentration NH 3 Concentration Amount NH 3 (ppm) Adsorbed (mmoles per g) 200 0.63 500 1.22 1000 1.48 5 The means to make the supply of ammonia intermittent during the engine cycle in the present apparatus can be a switch which switches the ammonia supply on and off dependent on the level of NOx conversion occurring over the SCR catalyst. Preferably, however, the means to make the supply of ammonia intermittent comprises a switch to switch on the means to supply the ammonia when the temperature of the catalyst rises above a set level (i) during the engine cycle, and to switch off the means to supply the ammonia when the temperature of the catalyst falls below a set level (ii). The set level (i) is preferably in the range 250-400°C, especially in the range 250-350°C. The set level (ii) is preferably in the range 200-250°C. The ammonia can be supplied for instance 1-30 times per minute. The source of ammonia and means to supply it from the source to the catalyst can be conventional. Compounds of ammonia as a solid or a solution in water are preferred. The compounds are preferably urea or ammonium carbamate. The means to supply the ammonia from the source to the catalyst can be a pipe through which it is injected into the exhaust gas up-stream of the catalyst. Thus, the present invention can be employed to provide a method of promoting the conversion of NOx under oxidising conditions in an exhaust fitted with a means of injecting NH 3 and a catalyst which adsorbs NH 3 during parts of the engine cycle in which the exhaust gas is sufficiently warmed for the hydrolysis of NH 3 precursor and injection of ammonia and ammonia is adsorbed by the catalyst for use as reductant for NOx during parts of the engine cycle in which the exhaust gas is cooler, without the need for the continuous injection of NH 3 into the exhaust gas. It can be seen that the invention provides an exhaust system for an engine operating generally under lean conditions, which exhibits a higher exhaust gas temperature and a lower exhaust gas temperature, the lower exhaust gas temperature being inadequate for the effective hydrolysis of NH 3 precursor and injection of NH 3 (generally a temperature below 200 °C), and an NH 3 SCR catalyst arranged and constructed so that during the higher exhaust gas temperature parts of the engine cycle the catalyst adsorbs NH 3 and during the lower exhaust gas temperature parts of the engine cycle the adsorbed NH 3 is used as reductant for NOx. The catalyst can be any which has the required characteristics of the present catalyst. The same material can both selectively catalyse the reduction and also adsorb and desorb the ammonia, and this is preferred. However, different materials in the catalyst can perform the two functions, one material catalysing and one material adsorbing and desorbing. When different materials are employed, they can be physically separate or, preferably, in admixture one with another. A zeolite can perform both functions or a zeolite can be employed which performs one function together with a different material, which may or may not be a zeolite, which performs the other function. The catalyst preferably comprises a zeolite. The zeolite can be metallised or non-metallised, and can have various silica-to-alumina ratios. Examples are metallised or non-metallised ZSM5, mordenite, γ zeolite and β zeolite. Preferred is ZSM5 or ion-exchanged or metal impregnated ZSM5 such as Cu/ZSM5. It may be desirable that the zeolite contains metal, especially Cu, Ce, Fe or Pt; this can improve the low temperature SCR activity. The zeolite can contain for instance 1-10% of metal by weight. The catalyst should have an appropriate structure, for instance in terms of pore size or surface acid sites, to trap and release NH 3 . The catalyst is preferably carried out on a support substrate, in particular a honeycomb monolith of the flow-through type. The monolith can be metal or ceramic. The substrate can be conventional. Nitrogen oxide (NO) is usually the most abundant nitrogen oxide in an engine exhaust stream, but at lower temperatures the reaction of the adsorbed NH 3 on a zeolite catalyst occurs more readily with NO 2 than with NO. Accordingly it is often desirably to oxidise NO to NO 2 up-stream of the SCR catalyst, particularly at low temperature. The present engine can be a diesel or petrol (gasoline) engine. The diesel engine can be a light duty or heavy duty diesel engine. The engine is preferably that of a vehicle. 7 The invention is illustrated by the accompanying drawings, which are graphs in which: Figure 1 shows NOx and NH 3 concentrations in simulated exhaust gas against temperature after treatment by zeolite ZSM5, the NH 3 being supplied continuously; Figure 2 shows the temperature programmed desorption (TPD) of NH 3 from ZSM5 which had been pre-adsorbed at 100°C, the graph showing, in arbitrary units, the concentration of ammonia in the gas against temperature; Figure 3 shows the NH concentration in a full simulated exhaust gas mixture containing 4.5% CO 2 , 12% O 2 , 4.5% H 2 O, 200ppm CO, 1 OOppm C 3 H 6 , 20ppm SO 2 and 200ppm NH 3 with the balance N 2 after passage over ZSM5 at 250°C against time, and hence shows the NH 3 uptake by the zeolite; Figure 4 shows the NOx concentration remaining in simulated exhaust gas after passage over the zeolite containing adsorbed NH 3 resulting from the adsorption shown in Figure 3 against time; Figure 5 shows the NOx concentration remaining in simulated exhaust gas containing 200ppm NO, 200ppm CO, 12% O 2 and 14% CO 2 with the balance N 2 after passage over ZSM5 with and without pre-adsorption of NH 3 against temperature; Figure 6 shows the corresponding effect to that shown in Figure 5 of successive cycles of the NH 3 pre-adsorption followed by subjection to the simulated exhaust gas; Figure 7 corresponds to Figure 5 but with the simulated exhaust gas containing also hydrocarbon; Figure 8 corresponds to Figure 7 but with the simulated exhaust gas containing also H 2 O and SO 2 ; Figure 9 corresponds to Figure 5 but with the simulated exhaust gas containing NO 2 instead of NO; Figure 10 corresponds to Figure 9 but with the simulated exhaust gas containing also hydrocarbon; Figure 11 corresponds to Figure 10 but with the simulated exhaust gas containing also H 2 O and SO 2 ; Figure 12 shows NOx concentration and temperature against time during part of an engine cycle; 8 Figure 13 corresponds to Figure 12 but shows the effect of intermittent supply ' of NH 3 ; Figure 14 shows the NOx concentration remaining in simulated exhaust gas after passage over Cu/ZSM5 with and without pre-adsorption of NH 3 against temperature; and Figure 15 shows the NOx concentration remaining in simulated exhaust gas which is that used in relation to Figure 14 but containing also hydrocarbon, H 2 O and SO 2 , after passage over Cu/ZSM5 with pre-adsorption of NH 3 against temperature. Figures 1-4 are discussed further hereinbefore, and Figures 5-15 hereinafter. The invention is illustrated also by the following Examples. EXAMPLE 1 Reaction of NO With Pre-adsorbed NH 3 Over Non-metallised ZSM5 This Example shows the effect of pre-adsorbing NH 3 at 250°C on the conversion of NOx over a non-metallised zeolite in a simple gas mixture containing NOx, CO, C0 2 and O 2 during a light-off test from room temperature to 400 °C. The gas stream containing NO (200ppm), CO (200ppm), O 2 (12%), CO 2 (14%) with the balance N 2 at a flow rate of 2 litres per minute was first passed over the non-metallised zeolite (0.4g) from room temperature to 400°C at a heating rate of 50°C per minute and the NOx at the outlet measured. In a subsequent experiment, the catalyst temperature was first raised to 250°C and 200ppm NH 3 was added to the gas stream, the zeolite was exposed to that stream for 5 minutes and then the NH 3 switched off, and the catalyst was cooled to room temperature and the rapid light- off repeated. Figure 5 shows the outlet NOx concentration for these experiments. It can be seen that in the case where NH 3 was not pre-adsorbed over the catalyst, some of the NOx is adsorbed on the zeolite at low temperature and is then subsequently released between 150°C and 350°C, but that when NH 3 was pre-adsorbed on the zeolite, the zeolite did not adsorb a significant amount of NOx at low temperature. Furthermore, it can be seen that a decrease in the outlet NOx concentration occurs from 150°C to 450°C due to the reaction of the NOx with the pre-adsorbed NH 3 . This effect of reacting the adsorbed NH 3 with the NOx can be repeated over successive cycles with NH 3 injection at 250°C between each cycle, as is shown in Figure 6. We have also shown that even in the presence of other gaseous components such as hydrocarbon, H 2 O and SO 2 , the adsorption of NH 3 will readily occur on the zeolite and can be used to reduce NOx. For example, Figure 7 shows the effect of adding 200ppm C 3 H 6 to the gas mixture in similar tests to those described above and Figure 8 shows the effect of further addition of H 2 O (10%) and SO 2 (20ppm). It can be seen that in both cases NOx was reduced by the adsorbed NH 3 . EXAMPLE 2 Reaction of NO 2 with Pre-adsorbed NH 3 Over Non-metallised ZSM5 The selective catalytic reduction of NOx by NH 3 under oxidising conditions proceeds more rapidly at low temperature if NO 2 instead of NO is present. The present Example shows that NH 3 pre-adsorbed on a zeolite catalyst can be used to reduce NO 2 even at a temperature as low as 100°C. This was demonstrated by rapid light-off tests analogous to that described above in Example 1. In the first experiment, a simple gas mixture containing NO 2 (200ppm), CO (200ppm), O 2 (12%), CO 2 (14%) with the balance N 2 at a flow rate of 2 litres per minute was passed over the non-metallised zeolite (0.4g) from room temperature to 400 °C at a heating rate of 50 °C per minute. In a subsequent experiment, the catalyst temperature was first raised to 250 °C and 200ppm NH 3 was added to the gas stream, the zeolite was exposed to that stream for 5 minutes and then the NH 3 was switched off, and the catalyst was cooled to room temperature and the rapid light-off repeated. Figure 9 shows the outlet NOx concentration from these experiments. It can be seen that in the absence of pre-adsorbed NH 3 , NO 2 is adsorbed at low temperature over the zeolite and is released between 100°C and 300°C, but when NH 3 was pre-adsorbed on the catalyst, significant NOx reduction is shown over the entire temperature window up to 400 °C. We have also shown that even in the presence of hydrocarbon, H 2 O and SO 2 adsorbed NH 3 will readily react with NO 2 . Figure 10 shows the effect of adding C 3 H 6 on the reaction 10 of pre-adsorbed NH 3 with NOx, and Figure 11 demonstrates the effect with addition of H 2 0 and SO 2 . EXAMPLE 3 Reaction of NO. With Pre-adsorbed NH 3 Over Non-metallised ZSM5 in Cvcle Test In most cases, exhaust gas temperature varies during an engine cycle and for a significant fraction of that time the temperature can be low. We have shown that by injecting NH 3 over a set temperature during the cycle, the adsorbed NH 3 can subsequently be utilised in reducing NOx at both low and high temperature. In the experiment, exhaust gas containing CO 2 (14%), O 2 (12%), H 2 O (10%), CO (200ppm), C 3 H 6 (200ppm), SO 2 (20ppm) and N0 2 (200ppm) was cycled between 150°C and 350°C with a dwell of approximately 5 minutes at 250°C during the cooling-down part of the cycle. The NH 3 injection was switched on when the temperature was at 350° C and switched off when the temperature fell to 250°C. Figure 12 shows the outlet NOx concentration and the temperature against time without any NH 3 injection, and Figure 13 shows the effect of the cycling with the intermittent injection of NH 3 . In both Figures, the ordinate scale gives the degrees C for the temperature graph and the parts per million (ppm) for the NOx graph. EXAMPLE 4 Reaction of NO With Pre-adsorbed NH 3 Over Cu/ZSM5 This Example shows the effect of pre-adsorbing NH 3 at 250°C on the conversion of NOx over a Cu-impregnated ZSM5 (containing 5% copper by weight) in a simple gas mixture containing NOx, CO, CO 2 and O 2 during a light-off test from room temperature to 400°C. The gas stream containing NO (200ppm). CO (200ppm), O 2 (12%), CO 2 (14%) with the balance N 2 at a flow rate of 2 litres per minute was first passed over the Cu/ZSM5 (0.4g) from room temperature to 400°C at a heating rate of 50°C per minute and the NOx at the outlet measured. In a subsequent experiment, the catalyst temperature was first raised to 250 °C and 200ppm NH 3 was added to the gas stream, the Cu/ZSM5 was exposed to that stream for 5 minutes and then the NH 3 was switched off, the catalyst was cooled to room 11 temperature rapidly and the light-off repeated. Figure 14 shows the outlet NOx ' concentration for these experiments. It can be seen that in the case where NH 3 was not pre- adsorbed on the catalyst, some of the NOx is adsorbed on the zeolite at low temperature, and is then subsequently released at higher temperature, but the pre-adsorption of NH 3 at 250°C suppresses the amount of NOx adsorbed at low temperature, with significant NOx reduction by the pre-adsorbed NH 3 at temperatures greater than 125 °C. Similarly, even in the presence of other gaseous components such as hydrocarbon, H 2 O and SO 2 the adsorption of NH 3 will occur readily over the Cu/ZSM5 and can be used to reduce NOx. For example, Figure 15 shows the effect of pre-adsorbing NH 3 on the Cu/ZSM5 at 250°C from a gas mixture containing NO, H 2 0, C0 2 , CO, C 3 H 6 , S0 2 and O 2 and the reduction of NOx by the adsorbed NH 3 during a light-off test.

Claims: 12 CLAIMS 1. Apparatus for reducing the content of nitrogen oxides (NOx) in the exhaust gas of a lean bum engine, which apparatus comprises: (a) exhaust apparatus through which the exhaust gas flows; (b) selective catalytic reduction catalyst in the exhaust apparatus, the catalyst catalysing the reduction of the NOx by ammonia to nitrogen and adsorbing and desorbing ammonia during the engine cycle; (c) a source of the ammonia; (d) supply means to supply the ammonia from the source to the catalyst; and (e) means to make the supply of ammonia intermittent during the engine cycle; whereby the catalyst adsorbs ammonia during its supply and the ammonia which has been adsorbed reacts with the NOx when the ammonia is not supplied. 2. Apparatus according to claim 1 adapted to pass the exhaust gas continuously over the catalyst. 3. Apparatus according to claim 1 or 2 wherein the means to make the supply of ammonia intermittent during the engine cycle, (e), comprises a switch to switch on the supply means, (d), when the temperature of the catalyst rises above a set level, (i), during the engine cycle, and to switch off the supply means, (d), when the temperature of the catalyst falls below a set level, (ii). 4. Apparatus according to claim 3 wherein the set level (i) is in the range 250-400°C and the set level (ii) is in the range 200-250°C. 5. Apparatus according to any one of claims 1 -4 wherein the catalyst comprises the same material which both selectively catalyses the reduction and also adsorbs and desorbs the ammonia. 13 6. Apparatus according to any one of the preceding claims wherein the catalyst comprises a zeolite. 7. Apparatus according to claim 6 wherein the zeolite is non-metallised. 8. Apparatus according to claim 7 wherein the zeolite is ZSM5. 9. Apparatus according to claim 6 wherein the zeolite contains metal. 10. Apparatus according to claim 9 wherein the zeolite is Cu/ZSM5. 11. A method of reducing the content of nitrogen oxides (NOx) in the exhaust gas of a lean bum engine, which method comprises passing the exhaust gas over a selective catalytic reduction catalyst which catalyses the reduction of the NOx by ammonia to nitrogen and which adsorbs and desorbs ammonia during the engine cycle, ammonia being supplied intermittently to the catalyst during the engine cycle, the catalyst adsorbing ammonia during its supply and the ammonia which has been adsorbed reacting with the NOx when the ammonia is not supplied.

Inventors: CHANDLER GUY RICHARD, GOERSMANN CLAUS FRIEDRICH, RAJARAM RAJ RAQ, SELF VALERIE ANNE, CHANDLER, GUY, RICHARD, GOERSMANN, CLAUS, FRIEDRICH, RAJARAM, RAJ, RAQ, SELF, VALERIE, ANNE
Applicants: CHANDLER GUY RICHARD, GOERSMANN CLAUS FRIEDRICH, JOHNSON MATTHEY PLC, RAJARAM RAJ RAQ, SELF VALERIE ANNE, CHANDLER, GUY, RICHARD, GOERSMANN, CLAUS, FRIEDRICH, JOHNSON MATTHEY PUBLIC LIMITED COMPANY, RAJARAM, RAJ, RAQ, SELF, VALERIE, ANNE
Application year: 1999
Main classification: B01D53
IPC codes: B01D53, F01N3