METHOD FOR THE OXIDATION OF LIQUID OR SOLID POLLUTANTS IN GAS STREAMS

Abstract: The invention relates to a method for the oxidation of carbon- and/or hydrocarbon- and/or combustable organic compounds containing liquid or solid particulate contaminants in gas streams, more in particular soot in exhaust gasses of diesel engines, comprising the treatment of said gas streams in a turbulent flow precipitator, of which at least part of the surface shows catalytic activity for non-selective oxidation.

Description: METHOD FOR THE OXIDATION OF LIQUID OR SOLID POLLUTANTS IN GAS STREAMS Title: Method for the oxidation of carbon- and/or hydrocarbon- and/or organic compounds containing liquid or solid particulate contaminants in gas streams. The invention relates to a method for the oxidation of carbon- and/or hydrocarbon- and/or organic compounds containing liquid or solid particulate contaminants in gas streams, more in particular on the diminishing, or the prevention of soot emission from li. a el engines, comprising the treatment of the soot containing exhaust gasses prior to their emission to the open air. Emission of gas streams which are contaminated with soot particles or with particles of solid or liquid hydrocarbon or organic compounds (for example oil or fat droplets) to the atmosphere is undesirable. This problem can be found in many places, such as in the oil processing industry and the like. It is known also that diesel engines show the disadvantage of a relatively high emission of soot particles. These soot particles have a negative influence on the environment and much research has been done already into the diminishing of the soot emission of diesel engines. A first possibility is to operate the engine at such conditions that the soot formation diminishes. In general this can be done at the expense of the capacity, the power and the fuel expenditure of the engine. An other possibility is the removal of the soot particles that are formed from the exhaust gasses. However, in this last case one meets the difficulty that it is not easy to collect and to convert the often very fine particles . The present invention aims at providing a method to diminish or even prevent the emission of such pollutants, by separating the solid or liquid particles from the exhaust gasses and by burning these after their separation through application of a non-selective oxidation catalyst (combustion catalyst?) in the separator. Therefor the invention relates to a method for the oxidation of carbon- and/or hydrocarbon- and/or organic compounds containing liquid or solid particulate contaminants in gas streams, comprising the treatment of said gas streams 5 in a turbulent flow precipi tator , of which at least part of the surface area shows catalytic activity for non-selective oxidation. More in particular the invention relates to a method for the diminishing, or the prevention of soot emission of diesel 10 engines, comprising the treatment of soot containing exhaust gasses orior to their jnission ir. the BPΠ lir i v i turbulen flow recipitator . of which -i least par" ot the surface ired shows catalytic activity for non-selective oxidation. The invention is based on the application of the 15 principle of a specific separation system for the separation of very fine particles from gas streams, a 'Turbulent Flow Precipitator ' , as described for instance in the internationai patent application WO-A 93/15822, in combination with a catalytic combustion of the captured (soot) particles. 20 The separation is based on the phenomenon that a turbulent gas stream in a space, near to the walls of this space shows a zone of decreasing turbulence, known as the viscous border zone. In this zone particles can be captured and removed. According to the method described in said 2.3 international patent application one obtains ■ 3e , o«ration of ^articles of a dimension of 0.01 to 100 microme er in a separator by passing the turbulent gas stream over a series of vertical plates, which form a number of vertical spaces with a chink (slit) form, which are in direct contact with the space 30 in which the turbulent gas stream is contained. The present invention is based on the insight that, it is possible to oxidize the mostly organic or soot particles, by bringing these in contact with a combustion catalyst (a non- selective oxidation catalyst) in said separation spaces of a 35 slit (chink) form. It is known that for a good oxidation a good contact is necessary between the particles and the catalytically active material. In a separator of said type one obtains such a said good contact, especially if use is made of a preferred design of the separator and a preferred composition of the catalysts to be described later on. According to the invention one takes care that in the separating spaces (slits/chinks) , that is to say in the zone in which the main gas stream is not conveyed, a combustion catalyst is present. Herewith it is of importance that catalytically active surfaces are present in said slits/chinks. This surface can be provided by the surface of the plates, or as a packing in the slits/chinks. The surface can already be cataly ically active from origin or can be nade active through the nature or. the construction material of the plates or the packing ''for instance copoer) . However, it is also possible to rovide the catalytic activity by the application of a catalytically active material on said surface, for example as a wash coat. Preferably the separator is provided with a packing, which exists of a metallic or ceramic support material, of which the surface already shows or gains catalytical activity for non-selective oxidation. According to a preferred method of the invention one doesn't apply the design described above, but an improved design which is described in the dutch patent application Nl 10-01963 of the same date. In this application an apparatus is described, which consists of at least a housing provided with an entrance duct for the gas stream to be purified on the one side fend) and a discharge (exit) duct for the purified gas stream on the other side (end), as well as at least one predominantly vertically placed convey channel for said gas stream, at which said apparatus is provided with means for the separation of the particles from said gas stream, which means are bounded to the convey channel, are in direct contact therewith and consist of a number of plates which are directed at an angle smaller than 90 degrees with the convey axis and where again and again two plates form a chink (crevice, slit) , which is fit for separating and discharging the particles. The conveying of the gas takes place either in upward or in downward direction, at which it is also possible to connect two or more vertically mounted pipe parts by bends of about 180 degrees, which shows as advantage that the system needs less height. With a system as described above an optimal separation of the particles is obtained, while simple combustion of these particles is also possible, for instance by providing the surface of the plates, on which the particles fall, with a combustion catalyst. An other possibility is the application of a packing material consisting of a predominantly inert nateriai . for instance a netal or a ceramic material, on the surface of which a catal tically active material is applied, or a packing material which itself shows catalytic activity. Under the influence of the gravitational force, or by mechanical vibrations, for instance resulting from the engine of a diesel vehicle, the particles will always move downward, so that the contact between the particles and the catalytically active surface is warranted almost always. It is known that in existing systems for the removal and combustion of soot from exhaust gasses the warranty of this contact is problematic. The contact between the separated soot and the catalyst is an essential condition for a good combustion of the capured soot. This is decribed. among others, in publications of J.P.A. \eeft et al . in the contents of which is contained herein as a reference. In this reference it is described that a good contact between the soot and the catalyst, as is obtained for instance by mixing of soot and catalyst in a ball mill, results in an appreciably (up to 200 °C) lower temperature of combustion than in case of bad contact as this results from mixing of soot and catalyst by shaking. Experiments, in which the combustion temperature was determined for soot, emitted by a diesel engine and captured on a ceramic filter provided with a layer of combustion catalyst, it was found that this temperature almost coincides with the combustion temperatures in case of bad contact. As a packing material one can use almost any material that is resistant to the conditions prevailing at the oxidation. Examples are various kinds of fibres, (ceramic, metallic, glass), catalysts support particles, metallic and ceramic packings, or metallic and ceramic monoliths. Due to the temperature of the exhaust gasses the separator automatically gets the temperature necessary for combustion, whilst the composition of the exhaust gasses can be chosen or adapted problemless in such a way that sufficient oxygen is present for the combustion. Using gas streams of other origins one has evidently to provide for the correct temperature and for sufficient oxygen. As catalytic materials use is made preferably of materials which are known as combustion cat lysts (non- selective oxidation catalysts) like copper, vanadium, chromium, manganese, molybdenum, platinum, palladium, tungsten, iron, cobalt, silver, alkali inetals, earth alkali metals, cerium, lanthanum, lead, nickel as well as combinations and/or compounds thereof. The application of the catalytic surface can be performed in known ways, at which more in particular attention can be given to a washcoat, precipitation, impregnation, but also to vacuum or electrolytic deposition of a metal, purposely followed by conversion into the catalytically active form. The catalytically active material preferably consists of a mixture of metal salts and/or oxides and/or compounds which at the working temper ture of the convertor, i.e. general I at T > 250-300 C C, are totally or partially molten, depending on the working conditions of the diesel engine and of the insulation measures taken for the exhaust system and the convertor. The captured soot particles are wetted by the melt. In this way a continuous and optimal contact of the catalyst and the soot particals to be combusted is obtained, quaranteeing an optimal combustion (conversion) and combustion velocity of the soot. The absolute necessity of the physical contact between the soot particals and the active catalytic material in the catalyst particles for the oxidation of the soot is described, among others, in the publication •of J.P.A. Neeft et al. mentioned above. If no particular measures are taken to maintain this contact during the progress of the oxidation reaction the oxidation velocity can decrease because the contact surface area between the soot and the catalytically active material diminishes by the oxidation reaction or ceases completely. Mixtures which are completely or partially molten at the said low temperatures are for instance mixtures of the oxides of molybdenum, vanadium and alkalimetals . Another mixture is for instance based on boric acid and boric oxide. To said mixtures additional metals and/or metal ions can be added to enhance the rate of oxidation of the soon respect Ivelv hhe transfer of oxygen from the gas phas. to the melt and/or fron the melt to the soot particles. Here one can think of the addition of copper, platinum, palladium, tungsten, chromium, manganese, iron, cobalt, nickel, lead, silver, cerium, lanthanum, and rare earth metals, as well as of combinations and/or compounds thereof, but the listing is not restricted to this. The melting point of a number of interesting low melting mixtures of alkali/molybdenum/vanadium oxides and of boric acid/boric oxide, as listed for instance in "Gmelin's Handbuch der Anorganische Chemie", is given as an example in the table 1, but is not restricted to this. TABEL 1 T ( Eutec t ) mo l e* rao l eX • c CsVOj 75 . 5 MoOj 24 . 5 362 V 2 0? 51 . 0 Cs jMoOi 49 . 0 352 Cr : (Mo ■o j 10 Cs 2 Mo0» 90 400 The separation of soot takes places in the exhaust system of the diesel engine, where preferably the vertically mounted design is applied. However, in. case that this is not allowed by the construction of the engine and/or the vehicle, one can also use a horizontally mounted system. In that case, the plates for the separation and the catalytic combustion are mounted preferably underneath the convey channel of the exhaust gasses. In that case, a possible design is a circular or elliptic pipe, which is provided with a gas convey channel at the upper side and further with predominantly vertically mounted separation plates in between which the combustion catalyst is applied. An important aspect of the invention is the fact that according to the invention the mayor part of the separated solids is converted into gaseous compounds which are removed from the system together with the exhaust gasses. In general it is preferred that a means is present for the removal of ash rests resulting from the combustion of the soot. In the system turbulence is obtained and maintained by a combination of velocity (generally > 5 m/s) and diameter (hydraulic diameter) of the convey channel. Preferably the gas stream is turbulent already at the entrance of the apparatus thus making additional measures unnecessary. Only when the parameters which determine the turbulence (velocity, diameter, density, viscosity) change during the transit it can be necessary to take additional measures to maintain or enhance the extent of turbulence. Said measures are among others the installation of plates which restrict the transit area. Generally one can say that sufficient separation can e obtained if one takes care that the Reynolds number in the centre of the convey channel is larger than 2000. As a result of the decreasing turbulence near the wall of the convey channel the particles collect there and they will be captured in between the downwardly pointing plates, where their conversion into C0 2 and eventually HjO takes place with the aid of the catalytically active material and oxygen. It is of importance that the sloping plates are mounted in such a way that the solid material, through a correct choice of the angle of the plates with the horizontal, makes contact with the catalytically. active surface through the action of gravity. The invention relates also to a(n) apparatus/means which is fit for the execution of the method, which means consists of at least a housing provided with an entrance duct for the (exhaust) gasses to be cleaned on the one side (end) and a discharge (exit) duct for the purified gasses on the other side (end), as well as at least one convey channel for said (exhaust) gasses, in which said apparatus/means is provided with means for the separation of the particles from said (exhaust) gasses, which means are bounded to the convey channel (s). are in direct contact therewith and consist of a number of plates, where again and again two plates form a chink (crevice, slit) in between each other, forming a zone in which no net gas flow occurs, which zone is fit for catching (capturing) and discharging particles contained in the (exhaust) gasses, where in said zone a catalytically active surface is present for the non-selective oxidation of the particles (soot) . Now, the invention is elucidated with the aid of figures, in which: Figure 1 shows three schematic representations of sections of the apparatus, in which figure IA and IB apply to a (predominantly) vertically mounted apparatus and figure IC applies to a (predominantly) horizontally mounted apparatus, in which it is of importance for the choice of the direction of the slope of the plates (dishes/cones) that the captured (soot) particles are brought and stay in contact by gravitational forces with the catalytically active material which is applied on or in between the plates. Figure 2 shows a sextet of possible shapes of the plates (dishes/cones) of the apparatus given in figure IA. Figure 3 shows a pair of possible shapes of the plates (dishes/cones) for the apparatus given in figure IB. Figure 4 shows a concentrical multichannel design. In figure IA and IB (1) is the, predominantly vertical, axis of symmetry of the revolved body, the cone, with a circular ground plane or a regular polyhedron with a three or more fold symmetry around this axis, as indicated in figure 2. The annular channel (2) that is formed between the housing (4) and the stacking of plates (cones) (3) in figure IA serves as channel for the conveying of the exhaust gasses which can flow either upwardly or downwardly. The direction of flow of the exhaust gasses through the central channel (5) which is formed by the periferical cones (plates) (6) in figure IB can be chosen freely as well. In figure IB the housing (4) and the cones (6) fit seamless to each other by seam(packing) (13) so that no bypass stream can occur in the (soot) particle collecting spaces (9). In figure IC the axis (7) of the housing (4) is predominantly in horizontal direction. The plates or dishes (10) are provided with holes (savings) (8) forming a channel (11) through which the exhaust gasses to be cleaned are conveyed. The plates (10) fit seamless to the housing (4) with the aid of seam (13) so that no bypass stream can occurs. The captured (soot) particles are collected in the (soot) collecting spaces (9) which are formed in between two consecutive plates and in which in some way material is present allowing for the catalytic oxidation of the (soot) particles. The constructions are provided with an entrance and an exit duct (12). which may change their function depending on the direction of flow of the gas. In the figures 2A up to and including 2F are indicated revolved bodies which may serve as plates (cones/dishes) in the apparatus shown in figure IA. However, the shape of the plates is not restricted to these shown. In the figure 2A up to and including 2D the plates are obtained by revolving a straight line (2), a bend line (3), and a broken line (4), and the broken line (5) , respectively, around the axis of symmetry (1) on which the origin of these lines is situated, whilst in the figures 2E and 2F revolved bodies are drawn which possess an N-fold axis of symmetry, where in said drawing N is chosen equal to N = 6. In figure 2E (6) is one of the planes of the cone body, whereas in figure 2F the planes (7A) , (7B) and (7C) are one of the composed side planes of the N-fold symmetrical body, where N is taken equal to N = 6. To obtain a regular flow of the exhaust gasses to be cleaned it is preferred that the (shape of the) cross section of the housing is the same as these of the cones. So, the housing (9) in the figures 2A, 2B, 2C and 2D is a pipe with a circular cross section of which the axis coincides with the axis of symmetry (1), whilst in figures 2E and 2F the cross section of the pipe shaped housing (10) is a regular polygon with an N-fold symraetrv, where in the figure \ τ is chosen equal to N = 6. and the axis of the pipe coincides with the N-fold axis of symmetry. Figure 3A shows topped cone shaped bodies (6) which serve as plates in the pipe shaped housing (4) of which the axis (1) coincides with the axis of symmetry of the cone bodies and where (5) are a dust and gas tight seams between the housing (4) and the plates (6) . In between the upper side of the plates (6) and the housing (4) a space (9) is formed in which the captured particles collect and can continuously make contact with the catalytic material (11), which is present in that space, as a result of the gravitational force. The gas stream out of which the particles are separated can be conveyed through the channel (13) which is formed by the stacking of the topped cones (6). both in upward and in downward direction. In figure 3B an identical situation is drawn for a cone body having an N-fold symmetry axis, where N is taken equal to N * 6, and at which both the housing (10) and the plates (12) have a coinciding axis of symmetry (8) ; and seam (5) and (catalytic) packing (11) between the plates as well as gas conveying channel (13) have the same meaning as in the paragraph above. In figure 4 around a central axis (4) the central plates (2) are arranged, the ring shaped plates (3) and the periferic plates (4), in between which the gas conveying ring shaped- channels (5) are formed through which the exhaust gasses to be cleaned can flow either in upward or downward direction. In between the housing (7) and the periferic plates (4) a dust and gas thight packing (6) is installed. The plates can be provided with a (catalytic) packing (11) to promote the capturing efficiency and the oxidation of the captured (soot) particles. The (exhaust) gas stream to be cleaned is let through the apparatus via the inlet and exit ducts (12) which can change their function, depending on the direction of flow of the gas through the apparatus. A number of comparative experiments was performed showing the superior performance of catalytic systems which are at least partially molten at the temperature applied for the oxidation of the soot. To this end soot-catalyst mixtures were prepared by mixing in a ball mill to obtain good contact or in a tumble mixer to obtain poor contact. The mixtures obtained were put into a quartz glass reactor and enclosed in between inert beds of silicon carbide. In the catalyst bed a thermocouple was inserted to allow for the registration of the temperature during the reaction. The reactors made up in that way were together put in a furnace where through each reactor was let a mixture of 10 vol oxygen in argon, as a representative substitute for the about 10 vol% oxygen containing diesel exhausts. Then the temperature of the oven was set at a constant temperature, for instance 375 "C, for 20 hours. The concentrations of CO and C0 2 present in the exhausts were continuously monitored with the aid of an infrared spectrometer. Based on this the conversion and the reaction velocity of the soot were calculated. The material balances showed to be within 51 in all cases. Experiments were done with the following catalysts: Catalyst 1. Fe 2 0j, prepared by calcination of iron nitrate at 400 'C during 3 hours. Catalyst 2. CsVOj-MoOi, prepared by sintering a mixture of Cs 2 C0j and V 2 0i at 450 °C and subsequently melting at 600 °C, after which the amount of MoOj is added which is needed to obtain the eutectic mixing ratio, and this mixture was heated again to a temperature 100 *C above the melting point. The mass obtained was broken and sieved after cooling. Catalyst 3. CsV0j-Mo0)-Ce0 2 , prepared by the addition of 10 % weight Ce0 2 to the eutectic mixture of catalyst 2, melting, cooling, breaking and sieving. Catalyst 4. Cs 2 MoO»-Vjθ5-Ag 2 0, prepared by heating of the eutectic mixture of Cs?MoOι-V : 0< after the addition of 25 weight of Ag 2 0 to a temperature of 100 'C above the melting point. The Cs;Mo0: va. prepared in advance by sintering of a stoechio etric mixture of Cs-carbonate and Mo0) at 750 J C during 18 hours. The following experiments (Table 2) were performed in which in each a mixture of 40 milligrams soot with an equal amount of catalyst was brought into the reactor. Table 2 Experiment catalyst contact 1 1 good (ball mill) 2 1 poor (tumble mixer) 3 2 poor 4 3 poor 5 4 poor The results are shown in the accompagnying figuur 5. It appears clearly that catalyst 1 in poor contact with the soot (experiment 2) shows no measurable reaction whereas in case of good contact (experiment 1) a reasonably fast reaction occurs in the beginning, up to about 20 % conversion, after which the reaction velocity decreases rapidly, till no longer measurable anymore at 80 % conversion, as a result of the diminishing or ceasing of the contact between the soot and the catalyst. The reaction velocities as measured for the catalysts 3, 4 and 5 as a function of the degree of conversion decrease gradually as a result of the decrease of the amount of soot present due to its oxidation. It is clear that a very high conversion of the soot is reached in all these cases at a very high reaction velocity, that is to say in relatively short times of reaction. A comparison of the decrease of the reaction velocities for catalysts 3 and 4 in relation to the degree of conversion shows absolutely clearly that the addition of cerium oxide as promotor to the catalyst system has a very beneficial effect on the reaction velocity.

Claims: Claims: 1. Method for the oxidation of carbon- and/or hydrocarbonand/or combustible organics containing liquid or solid particulate pollutants in gas streams, comprising the treatment of said gas streams in a turbulent flow precipitator, of which at least part ofthe surface shows activity for non-selective catalytic oxidation. 2. Method for the diminishing, or preventing ofthe emission of soot from diesel engines, comprising the treatment ofthe soot containing exhaust gasses prior to their emission to the open air, in a turbulent flow precipitator, of which at least part ofthe surface shows catalytic activity for non-selective oxidation. 3. Method according to claims 1 or 2, in which the separator is provided with a packing.which exists of a support material of which the surface has activity for non-selective oxidation. 4. Method according to claims 1 -3, in which the catalytic activity is provided by one or more metals and/or compounds chosen from the group existing of copper, vanadium, chromium, manganese, molybdenum, platinum, palladium, tungsten, iron, cobalt, silver, alkali-metals, earth- alkali-metals, cerium, lanthanum, lead, nickel as well as combinations and/or compounds of that. 5. Method according to claim 3 or 4, in which the support material is a packing material consisting of-a mainly inert metal or ceramic material, of which on said surface a catalytically active material is applied. 6. Method according to claims 1 -5, in which the surface ofthe separator or ofthe packing material proper is catalytically active. 7. Method according to claims 1-6, in which the gas streams in the separator are, are brought and or are kept in turbulent flow, as a result of which the particles can be separated from said -as stream into a region where no net flow exists and which is in direct contact with said turbulent gas stream. 8. Method according to claims 1 -7,. in which the catalyst is at least partially molten at the workin - temperature ofthe separator. 9. Method according to claims 1-8, in, hich the catalytic activity is provided by a mixture, consisting of at least the metals and/or compounds and/or the oxides of V Mo/(earth) alkali, which is at least partially molten at the working temperature ofthe separator. 10. Method according to claim,9, in which the catalytic activity ofthe at least partially molten mixtures is increased by the addition of promoters, metals and/or metal ions and/or compounds of that, which enhance the transfer of oxygen from the gas phase to the catalytic mixture and/or from the catalytic mixture to the material to be oxidised, which promoters are chosen from the group copper, chromium, manganese, platinum, palladium, tungsten, iron, cobalt, nikkel, lead, silver, cerium, lanthanum, and rare earth metals as well as combinations and/or compounds of that. 1 1. Method according to claims I - 10, in which the catalytic activity is provided by a mixture of boric acid and boric oxide which is at least partially molten at the working temperature ofthe separator and to which is added at least one ofthe metals and/or compounds according to claim 4. 12. Apparatus suitable for the prevention and or diirώiishing of soot emission from diesel engines, which means consists at least of a housing provided with an entrance duct for the exhaust gasses to be treated on the one side and a discharge duct for the treated/cleaned exhaust gasses on the other side, as well as at least one convey channel for said exhaust gasses, in which the apparatus is provided with means for the separation ofthe soot particles from said exhaust stream, which means are bounded to the convey channel, are in direct contact therewith and consist of a number of plates, where again and again two plates form a chink (slit/crevice) which forms a zone in which no net gas flow exists which zone is fit for catching and removal of soot from said exhaust gasses where in said zone a catalytically active surface (area) for non-selective oxidation of soot is present.

Inventors: JELLES SYTSE JELLE, MAKKEE MICHIEL, MOULIJN JACOB ADRIAAN, VAN HARDEVELD RUDOLF, JELLES, SYTSE, JELLE, MAKKEE, MICHIEL, MOULIJN, JACOB, ADRIAAN, VAN HARDEVELD, RUDOLF
Applicants: HARDEVELD RUDOLF VAN, JELLES SYTSE JELLE, MAKKEE MICHIEL, MOULIJN JACOB ADRIAAN, STICHTING TECH WETENSCHAPP, UNIV DELFT TECH, JELLES, SYTSE, JELLE, MAKKEE, MICHIEL, MOULIJN, JACOB, ADRIAAN, STICHTING VOOR DE TECHNISCHE WETENSCHAPPEN, TECHNISCHE UNIVERSITEIT DELFT, VAN HARDEVELD, RUDOLF
Application year: 1996
Main classification: B01D45
IPC codes: B01D45, B01D53, B01J19, B01J23, F01N3