Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
  • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
  • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
  • B01D53/9404—Removing only nitrogen compounds
  • B01D53/9409—Nitrogen oxides
  • B01D53/9413—Processes characterised by a specific catalyst
  • B01D53/9422—Processes characterised by a specific catalyst for removing nitrogen oxides by NOx storage or reduction by cyclic switching between lean and rich exhaust gases (LNT, NSC, NSR)
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
  • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
  • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
  • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
  • F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
  • F01N3/10—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/206—Rare earth metals
  • B01D2255/2065—Cerium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/206—Rare earth metals
  • B01D2255/2066—Praseodymium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/207—Transition metals
  • B01D2255/20715—Zirconium

Definitions

• the present invention relates to a method for treating a gas containing nitrogen oxides (NOx), using as a NOx trap a composition based on zirconium oxide and praseodymium oxide.
• NOx nitrogen oxides
• NOx traps are systems capable of partially oxidizing and then storing the nitrogen oxides present in a poor gas, then destocking and reducing the same oxides to nitrogen when the surrounding mixture is rich.
• the known NOx traps still have some disadvantages, however.
• An object of the invention is therefore the development of an effective NOx trap in an area of low temperatures, below 40 ° C.
• Another object of the invention is to provide a NOx trap which, after sulphation can be regenerated or desulfated more easily, especially at temperatures below 600 ° C.
• the invention relates to a method for treating a gas containing nitrogen oxides (NOx), which is characterized in that a NOx trap is used based on a composition based on an oxidation catalyst. NOx to NO 2 and a compound based on zirconium oxide and praseodymium oxide in a proportion of praseodymium oxide of between 5% and 50% by weight of oxide.
• the NOx trap used in the process of the invention can be effective in a temperature range from 200 0 C to 300 0 C for example. This NOx trap can also be regenerated to a large extent at a temperature which can be as low as 550 ° C.
• NOx nitrogen oxides is meant the type oxide N 2 O, N 2 O 3 sesquioxide, pentoxide N 2 O 5, monoxide NO and nitrogen dioxide NO 2.
• specific surface is meant the specific surface B. AND. determined by nitrogen adsorption according to ASTM D 3663-78 established from the BRUNAUER-EMMETT-TELLER method described in the journal "The Journal of the American Chemical Society, 60, 309 (1938)".
• the process of the invention is characterized by the use as a NOx trap of a specific composition which will be described more precisely below.
• This NOx trap is a composition which firstly comprises a NOx oxidation catalyst to NO 2 .
• Catalysts of this type are known, they are generally metals and may be mentioned more particularly as catalysts of this type precious metals.
• Gold, silver, and platinum-bearing metals that is, ruthenium, rhodium, palladium, osmium, iridium, and platinum. These metals can be used alone or in combination.
• Platinum can be used particularly alone or in combination with rhodium and / or palladium and, in the case of an association, in majority proportion relative to the other metal or other metals.
• the amount of oxidation catalyst for example a precious metal, can be, for example, between 0.05% and 10%, preferably between
• the NOx trap of the invention comprises, as a support for this catalyst, a compound which is based on zirconium oxide and praseodymium oxide.
• a compound which is based on zirconium oxide and praseodymium oxide As indicated above, the proportion of praseodymium oxide in the compound is between 5% and 50%, it being understood that it is a proportion expressed by weight of praseodymium oxide P ⁇ On based on the total oxide weight of the compound. Below 5% the praseodymium oxide content is too low to observe a significant NOx trap effect. Above 50%, the thermal stability of the compound, that is to say the value of its specific surface at the temperatures at which it is used, becomes insufficient.
• the content of praseodymium oxide may more particularly be between 10% and 40%.
• the compound based on zirconium oxide and praseodymium oxide may further comprise cerium oxide, CeO 2 in particular.
• the proportion of cerium oxide may be such that the Ce / Zr atomic ratio is between 10/90 and 90/10. More particularly, this ratio can be at least 1.
• the compounds based on zirconium oxide and praseodymium oxide are known. They are described in particular in FR-A1 -2590887 which refers to a composition based on zirconium oxide and an additive which may especially be praseodymium.
• these compounds can be prepared by precipitation methods.
• a preparation by precipitation by addition of a basic compound such as ammonia to a solution of an acidic precursor of zirconium, for example a nitrate, chloride or zirconium sulphate, and a salt of praseodymium such as nitrate, chloride, sulfate or carbonate.
• a basic compound such as ammonia
• a salt of praseodymium such as nitrate, chloride, sulfate or carbonate.
• Another useful method is to mix a praseodymium salt with a zirconium hydrate sol, the suspension thus obtained is then dried. It is also possible to impregnate the zirconium oxide with a solution of a praseodymium salt.
• this area is at least 29 m 2 / g, after calcination at 1000 ° C. for 10 hours.
• these specific compounds may have a specific surface area of at least 45 m 2 / g.
• These compounds may in some cases be in the form of solid solutions of praseodymium in zirconium oxide.
• These compounds also have a specific porosity. They contain indeed mesopores, that is to say pores whose size is between 10 nm and 500 nm and this even after calcination at high temperature. These size values are obtained by mercury porosimetry
• the first step of the process therefore consists in preparing a liquid mixture of a zirconium compound and a praseodymium compound.
• the mixture is generally in a liquid medium which is water preferably.
• the compounds are preferably soluble compounds. It may be in particular zirconium salts and praseodymium. These compounds can be chosen for example from nitrates, acetates or chlorides.
• zirconyl nitrate or zirconyl chloride.
• Zirconyl nitrate is most commonly used.
• a soil as the starting compound of zirconium.
• sol any system consisting of fine solid particles of colloidal dimensions, ie dimensions of between about 1 nm and about 500 nm, based on a zirconium compound, this compound being generally an oxide and / or a hydrated oxide.
• the zirconium can be either totally in the form of colloids, or simultaneously in the form of ions and in the form of colloids.
• the starting mixture can be indifferently obtained either from compounds initially in the solid state which will be introduced later in a water tank for example, or even directly from solutions of these compounds and then mixture in any order of said solutions.
• said mixture is brought into contact with a basic compound.
• Hydroxide products can be used as base or basic compound. Mention may be made of alkali or alkaline earth hydroxides. It is also possible to use secondary, tertiary or quaternary amines. However, amines and ammonia may be preferred in that they reduce the risk of pollution by alkaline or alkaline earth cations. We can also mention urea.
• the basic compound is generally used in the form of an aqueous solution.
• the manner of bringing the mixture into contact with the solution, that is to say the order of introduction thereof is not critical. However, this introduction can be done by introducing the mixture into the solution of the basic compound.
• the bringing together or the reaction between the mixture and the solution, especially the addition of the mixture in the solution of the basic compound, can be carried out at once, gradually or continuously, and it is preferably carried out with stirring. It is preferably conducted at ambient temperature (20-25 ° C.).
• the next step (c) of the process is the step of heating the precipitate in a liquid medium.
• This heating can be carried out directly on the reaction medium obtained after reaction with the basic compound or on a suspension obtained after separation of the precipitate from the reaction medium, optional washing and return to water of the precipitate.
• the temperature at which the medium is heated is at least 100 ° C. and even more particularly at least 130 ° C.
• the heating operation can be carried out by introducing the liquid medium into a closed enclosure (closed reactor of the type autoclave). Under the conditions of the temperatures given above, and in aqueous medium, it is possible to specify, by way of illustration, that the pressure in the closed reactor can vary between a value greater than 1 Bar (10 5 Pa) and 165 Bar (1, 65. 10 7 Pa), preferably between 5 Bar (5 ⁇ 10 5 Pa) and 165 bar (1.65, 10 7 Pa). It is also possible to carry out heating in an open reactor for temperatures in the region of 100 ° C.
• the heating may be conducted either under air or under an inert gas atmosphere, preferably nitrogen in the latter case.
• the duration of the heating can vary within wide limits, for example between 1 and 48 hours, preferably between 2 and 24 hours.
• the rise in temperature is carried out at a speed which is not critical, and it is thus possible to reach the reaction temperature set by heating the medium for example between 30 minutes and 4 hours, these values being given for all purposes. indicative fact.
• the precipitate obtained after the heating step and possibly a washing may be resuspended in water and then another heating of the medium thus obtained may be carried out. This other heating is done under the same conditions as those described for the first.
• the next step (d) of the process consists in adding to the precipitate resulting from the preceding step a compound which is chosen from anionic surfactants, nonionic surfactants, polyethylene glycols, carboxylic acids and their salts and surfactants from type ethoxylates of carboxymethylated fatty alcohols.
• the addition of the surfactant can be done in two ways. It can be added directly to the precipitate suspension from the previous heating step (c). It may also be added to the solid precipitate after separation thereof by any known means from the medium in which the heating took place.
• the amount of surfactant used is generally between 5% and 100%, more particularly between 15% and 60%.
• the amount of surfactant in the precipitate suspension it is possible, after separation of the precipitate from the liquid medium, to carry out a washing of the precipitate thus obtained.
• the precipitate recovered is then calcined.
• This calcination makes it possible to develop the crystallinity of the product formed and it can also be adjusted and / or chosen according to the temperature of subsequent use reserved for the compound, and this taking into account the fact that the specific surface of the product is all lower than the calcination temperature implemented is higher.
• Such calcination is generally carried out under air, but a calcination carried out for example under inert gas or under a controlled atmosphere (oxidizing or reducing) is obviously not excluded.
• the calcination temperature is generally limited to a range of values between 500 ° C. and 1100 ° C., more particularly between 600 ° C. and 900 ° C.
• EP-A1-863846 describes a process for the preparation of this type of compound in which a liquid mixture containing a zirconium compound and a cerium IV compound is prepared; this mixture is heated to a temperature above 100 0 C; the reaction medium obtained at the end of the heating is brought to a basic pH; the precipitate thus obtained is recovered; and calcining said precipitate; the praseodymium being added either to the mixture in the starting liquid medium or to the reaction mixture obtained at the end of the heating.
• EP-A1-906244 also describes a process in which a mixture in a liquid medium containing a cerium compound, a zirconium compound and a praseodymium compound is prepared; said mixture is heated; the precipitate obtained is recovered and this precipitate is calcined, the aforementioned mixture being prepared using a solution of zirconium which is such that the amount of The base needed to reach the equivalent point in an acid-base assay of this solution satisfies the 0H7Zr molar ratio condition ⁇ 1.65.
• the oxidation catalyst of the type described above can be introduced into the composition of the invention by any known method, for example by impregnating the compound based on oxides with an aqueous solution containing the precursor of said catalyst such as an amine platinum complex. .
• gases that can be treated by the present invention are, for example, those from gas turbines, thermal power plant boilers or internal combustion engines. In the latter case, it may include diesel engines or gasoline engines operating in lean mixture.
• the composition used in the process of the invention functions as a NOx trap when it is contacted with gases having a high oxygen content.
• gas having a high oxygen content gases having an excess of oxygen relative to the amount necessary for the stoichiometric combustion of fuels and, more precisely, gases having an excess of oxygen relative to the stoichiometric value.
• ⁇ 1.
• gases are those of engine operating in lean bum and which have an oxygen content (expressed in volume) of at least 2%, as well as those with an even higher oxygen content, for example gases.
• engines of the diesel type ie at least 5% or more than 5%, more particularly at least 10%, this content may for example be between 5 and 20%.
• the NOx trap can sulphate due to the presence of sulfur in the fuels used for the operation of the engine. Therefore, the trap must from time to time be desulfated. This desulfation is done in a manner known to those skilled in the art by raising the temperature of the gases to be treated and by modifying the richness of these gases beyond the richness 1 (stoichiometry). However, in the case of the present invention, this temperature may be lower than those generally used. For example, it is possible to obtain, after a treatment at 550 ° C., an elimination of at least 50% of the sulfur adsorbed by the trap.
• compositions of the invention can be used in processes for treating gas resulting from the combustion of fuels with a high sulfur content, for example at least 350 ppm, more particularly at least 500 ppm, fuels of the type used for example in thermal power plant boilers.
• a high sulfur content for example at least 350 ppm, more particularly at least 500 ppm, fuels of the type used for example in thermal power plant boilers.
• NOx can be used in the form of powder but it can possibly be shaped to be in the form of granules, balls, cylinders or honeycombs of variable dimensions.
• the composition used as a NOx trap can be combined with complementary pollution control systems, such as three-way catalysts, which are effective when the value of ⁇ is less than or equal to 1 in gases, or to hydrocarbon injection or exhaust gas recirculation systems (EGR system) for diesel engines.
• This composition may also be used in a device comprising a coating (wash coat) based on the composition, on a substrate of the type for example metal monolith or ceramic.
• the invention therefore also relates to a device for implementing the method as described above and which is characterized in that it comprises as a NOx trap the composition which has been described above and based on of a precious metal and a compound based on zirconium oxide and praseodymium oxide.
• This device may be an exhaust line mounted on a motor vehicle with diesel engine or gasoline lean mixture and which includes a catalytic element which comprises this composition.
• This example relates to the preparation of a first compound that can be included in a composition that can be used in the process of the invention.
• This compound is based on oxides of cerium, zirconium and praseodymium in the respective proportions by mass of oxide of 55%, 15% and 30%.
• the acid-base dosage is in a known manner. To perform it under optimum conditions, a solution can be determined which has been brought to a concentration of approximately 3.10-2 mol per liter, expressed as zirconium element. A 1N sodium hydroxide solution is added with stirring. Under these conditions, the determination of the equivalent point (change in the pH of the solution) is clear. This equivalent point is expressed by the OH / Zr molar ratio. The concentration of this mixture (expressed as oxide of the various elements) is adjusted to 80 g / l. This mixture is then heated at 100 ° C. for 4 hours.
• the reaction medium thus obtained is boiled for 2 hours. After decantation and withdrawal, the solid product is resuspended and the medium thus obtained is treated for 1 hour at 100 ° C. The product is then filtered and then calcined for 4 hours at 800 ° C. in air. The product thus obtained has a specific surface area of 45 m 2 / g.
• This example relates to the preparation of a second compound that can be included in a composition that can be used in the process of the invention.
• This compound is based on 60% zirconium and 40% praseodymium, these proportions being expressed in percentages by weight of the ZrO 2 and Pr 6 Oi 1 oxides.
• the nitrate solution is introduced in one hour into the reactor with constant stirring.
• the solution obtained is placed in a stainless steel autoclave equipped with a stirrer.
• the temperature of the medium is brought to 150 0 C for 2 hours with stirring.
• the suspension thus obtained is then filtered on B ⁇ chner.
• a precipitate containing 19% by weight of oxide is recovered. 100 g of this precipitate are taken.
• an ammonium laurate gel was prepared under the following conditions: 250 g of lauric acid are introduced into 135 ml of ammonia (12 mol / l) and 500 ml of distilled water, and the mixture is then homogenized with using a spatula.
• the product obtained is then heated to 86 ° C. for 2 hours in steps. It then has a specific surface area of 61 m 2 / g.
• This example relates to the preparation of a third compound that can be included in a composition that can be used in the process of the invention.
• This compound is based on 90% zirconium and 10% praseodymium, these proportions being expressed in percentages by weight of the ZrO 2 oxides and
• Example 2 The procedure is the same as in Example 2 by mixing the nitrate solutions in the stoichiometric proportions required to obtain the above mixed oxide.
• the surface after calcination is 70 m 2 / g.
• This example relates to the preparation of a compound based on alumina and barium at 10% by weight.
• 5 g of Puralox alumina are introduced into a beaker and then covered with water (20 ml) before addition of the barium nitrate solution (10 ml to 50 g / l).
• the solution is evaporated in a sand bath while maintaining agitation.
• the solid is calcined at 700 ° C. under a 10% O 2 , 10% H 2 O, N 2 mixture for 4 hours.
• the specific surface area of the compound is 89 m 2 / g.
• This example gives the NOx storage capacity measurement results for 1% platinum catalyst compositions prepared from the compounds of the previous examples and in the following manner.
• the measurement of the NOx storage capacity is carried out under the following conditions:
• the catalytic composition as prepared above is introduced into a reactor and is then pretreated under oxidizing flux 10% O 2 + 5% N 2 in nitrogen for 30 minutes at a temperature of 200 ° C., then the reactor is isolated ,
• the reaction flow is then introduced into the catalytic test.
• the composition of the reaction stream is: 10% O 2 + 5% H 2 O + 600 ppm NO in nitrogen,
• composition of (NO + NO 2 ) of the reaction mixture is analyzed continuously by chemiluminescence with a COSMA Topaze 2020 analyzer,
• reaction stream is introduced into the catalytic reactor,
• composition of (NO + NO 2 ) at the outlet of the reactor is determined continuously by chemiluminescence
• the amounts of NOx stored are reported in Table 1.
• the catalyst compositions 1 to 4 of this table correspond respectively to the products obtained after impregnation with platinum, according to the process described above, of the compounds of Examples 1, 2 and 3 according to US Pat. invention and 4 comparative.
• compositions of the invention have a maximum of efficiency in the temperature zone of between 200 ° C. and 350 ° C., whereas this maximum is rather around 400 ° C. for the composition. comparative.
• This example relates to the regeneration after sulfation of the catalytic compositions of Example 5.
• the sulfation of the compositions is first carried out by treating them with a gas stream containing 60 ppm of SO 2 at a temperature of 300 ° C. for 5 hours. .
• compositions thus sulphated are then subjected to treatment with a reducing gas stream based on H 2 , CO 2 and H 2 O at a temperature of 550 ° C.
• the sulfur content of the sulfated compositions or after regeneration is determined by programmed temperature reduction (RTP) under a mixture containing 1% H 2 ; the composition of the gas phase is followed by chromatography with a differential detector.
• the catalyst sample is preoxidized under oxygen before RTP.
• the integration of the residual H 2 content at the outlet of the reactor makes it possible to determine the amount of hydrogen consumed to reduce the sulphate species.
• compositions of the invention have sulfur removal rates of at least twice that of the comparative composition.

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• 2005
  • 2005-09-12 FR FR0509275A patent/FR2890577B1/fr active Active
• 2006
  • 2006-09-08 JP JP2008530561A patent/JP2009507634A/ja not_active Abandoned
  • 2006-09-08 KR KR1020087008780A patent/KR20080066920A/ko not_active Application Discontinuation
  • 2006-09-08 WO PCT/FR2006/002069 patent/WO2007031627A1/fr active Application Filing
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