Apparatus and method for removing hydrocarbons from gaseous mixtures

Abstract: A method and system are disclosed for removing hydrocarbons from a gaseous mixture which comprises water and hydrocarbons which comprises contacting the mixture with a first stage comprising hydrophilic material to remove at least some of the water therefrom and produce a drier mixture, and thereafter contacting the drier mixture with a second stage comprising an agent for removing hydrocarbons, to produce a purified mixture.

Description: This invention relates to a catalyst system and method for removing hydrocarbons from a water-containing mixture which involves contacting the mixture first with hydrophilic material to at least partially dry the mixture, and thereafter contacting the mixture with an agent for removing hydrocarbons. The system and method are especially suited for removing hydrocarbons from auto exhaust. BACKGROUND OF THE INVENTION Internal combustion engines emit a large amount of unburned hydrocarbons. The hydrocarbons include low molecular weight alkanes and alkenes. Of these, the low molecular weight alkenes (olefins) are very troublesome because they have a great propensity to form ozone in the atmosphere and are most difficult to trap by adsorption. Ozone is a major smog forming constituent. For this reason, emission standards are becoming more stringent with regard to ozone-forming hydrocarbons. Internal combustion engines emit a large amount of unburned hydrocarbons during cold engine start-up. In fact, a substantial fraction of the total emitted hydrocarbons have been found to occur during the first ten seconds due to the rich fuel mixture. Release of hydrocarbons after starting an engine poses a special problem because at this point the temperature is not high enough for conversion to innocuous products in the presence of conventional catalysts. The catalysts utilized in catalytic converter systems are generally ineffective at ambient temperature and must reach high temperatures, often in the range of 300-400°C before they are activated. One method of reducing cold start emissions is to temporarily adsorb hydrocarbons on zeolites. One disadvantage of this method is that exhaust gas contains water which strongly inhibits the adsorption capacity of some zeolites, especially for olefins. DE-A-40 33 827 discloses an exhaust gas purification device for methanol-powered diesel engines. The device is composed of adsorption media specifically chosen to remove methanol and formaldehyde. Water vapor adsorbed by the adsorption medium increases the efficacy of adsorption of methanol and formaldehyde. The adsorption media is composed of an adsorber that has a strong adsorption capacity for water at 100°C. Therefore it would be desirable to have a hydrocarbon removal system in which water does not affect the adsorption of hydrocarbons. SUMMARY OF THE INVENTION In accordance with one aspect of the invention, there is provided a method for removing hydrocarbons from a gaseous mixture which comprises water and hydrocarbons, which comprises contacting the mixture with hydrophilic material to remove at least some of the water therefrom and produce a dried mixture, and thereafter contacting the dried mixture with an agent for removing hydrocarbons, to produce a purified mixture. In accordance with another aspect of the invention, there is provided a system for removing hydrocarbons from an exhaust gas mixture which comprises water and hydrocarbons. The system comprises a first stage comprising hydrophilic material for removing at least some of the water from the mixture to produce a dried gas mixture, and a second stage comprising a hydrocarbon-removing agent for removing hydrocarbons from the dried mixture, to produce a purified mixture. BRIEF DESCRIPTION OF THE FIGURE The Figure is a plot of quantity of adsorbed propylene versus time, for hydrocarbon-adsorbing systems in which several kinds of hydrophilic material are used, and for a system in which no hydrophilic material is used, for comparison purposes. DETAILED DESCRIPTION OF THE INVENTION This invention provides a system and method of removing hydrocarbons from a water and hydrocarbon-containing mixture in which first the water is removed by hydrophilic material and thereafter the hydrocarbons are removed by a hydrocarbon-removing agent. Especially suited to the practice of the present invention are gas mixtures which are released at start-up of internal combustion engines. Examples of hydrocarbons, although it is to be understood that the invention is not limited to these, are low molecular weight or light hydrocarbons found in gasoline, diesel fuel, alcohols, and their products of combustion and molecular rearrangements. Alkanes and alkenes with 1 to 6 carbon atoms are considered to be low molecular weight hydrocarbons. The invention is especially suited for low molecular weight alkenes (olefins). Some examples are ethylene, propylene, butadiene, pentene, and other unsaturated hydrocarbons. The invention is especially suited for removal of hydrocarbons having a Maximum Incremental Reactivity (MIR) of greater than about 1.0. The MIR is a measure of the propensity of a given hydrocarbon to form ozone expressed as grams ozone/gram of organic gas. The MIR is used in calculating the potential amount of ozone formed per mile for a specific hydrocarbon. In general, alkanes or paraffins have low MIR values (<0.5), aromatic compounds vary from <1 to about 10, and light alkenes or olefins especially ethylene, propylene and butadiene have very high MIR values of about 7.2 to about 10.8. Description of MIR values and a list of the MIR values assigned to various hydrocarbons is given in Technical Support Document entitled "Proposed Reactivity Adjustment Factors for Transitional Low-Emission Vehicles", September 27, 1991, Mobile Source Division, Research Division, California Air Resources Board, Part B, and Appendix A-1. The exhaust gas mixture contains typically about 2500 to 10000 volume ppm of hydrocarbons during the initial start-up period which is typically less than about 5 minutes, but this can vary. The hydrophilic material is one that preferentially takes up or adsorbs water from gas streams containing hydrocarbons and therefore functions as a drying agent. The hydrophilic material can be one or more of the following: molecular sieve, high surface area aluminas, precursors for high surface area aluminas, or high surface area silicas. Molecular sieves have pores defined by their crystalline structure. These pores must be large enough for the adsorption of water molecules and preferably small enough to prevent larger molecules from being adsorbed. It is preferred that the pore size of the molecular sieve be greater than about 0.2 nm (2 angstroms) in diameter, and preferably about 0.2 nm to about 0.5 nm (about 2 to about 5 angstroms) in diameter, and most preferably about 0.25 to about 0.4 nm (about 2.5 to about 4.0 angstroms) in diameter. Some hydrophilic materials that are especially suited for use as drying agents for hydrocarbon-containing gaseous mixtures are Types A, L, and X zeolites, chabazite, erionite, clinoptilolite, ferrierite, phillipsite, mazzite, offretite, aluminophosphates, and silicoaluminophosphates, and combinations of these. These types are meant also to include various ion-exchanged forms of these zeolites. Most preferred of these types of molecular sieves are KaA (Type 3A), NaA (4A), CaA (Type 5A), LiA, NaX (13X), K-erionite, phillipsite, and combinations of these. The preferred high surface area alumina is gamma alumina. Precursors for high surface area aluminas are those which form high surface area transition aluminas when they are fired. The preferred alumina precursors are alumina hydrates, such as gibbsite, bayerite, nordstrandite, boehmite, and diaspore. It is preferred that the surface area of the aluminas be at least about 50 m²/g, and preferably greater than about 200 m²/g. It is preferred that the high surface area silicas have a surface area of at least about 50 m²/g, preferably at least about 200 m²/g, and most preferably at least about 300 m²/g. The preferred high surface area silica is silica gel. The hydrocarbon removing agent can be any material which removes hydrocarbons from gas streams, such as by catalytic conversion, eg, cracking or oxidation, or sorption. Sorbing material or sorbing agents take up and hold substances by either absorption or adsorption. These constituents can then desorb under certain conditions which are predetermined. The term "sorbing material" or "sorbing agent" as used in the present invention can mean one or a plurality of sorbing agents. Adsorption is the taking up and holding of molecules by physical or chemical forces, termed respectively, physical or chemical adsorption. The term "adsorbing agent" according to the present invention means at least one adsorbing agent. There can be more than one type of adsorbing agent making up the hydrocarbon removing agent. Some typical adsorbing agents that are suited for removal of hydrocarbons are those that adsorb at relatively low temperatures and desorb at relatively high temperatures. For example, adsorbing agents that adsorb hydrocarbons at engine start-up temperatures which are typically less than about 150°C, and desorb at engine exhaust temperatures which are typically greater than about 150°C are especially suited to the practice of the present invention. Some typical hydrocarbon adsorbing agents which are especially suited to the practice of the present invention are molecular sieves, activated carbon, and combinations of these. Molecular sieves are crystalline substances having pores of size suitable for adsorbing molecules. Some types of molecular sieves which are preferred for the practice of the present invention are carbon molecular sieves, zeolites, metallophosphates, aluminophosphates, silicoaluminophosphates, and combinations of these. Carbon molecular sieves have well defined micropores made out of carbon material. Some preferred zeolites are faujasite type, especially preferred of which is ultra stable Y, (USY) preferably with SiO₂/Al₂O₃ mole ratios of greater than about 5, pentasil type, preferred of which are ZSM type such as ZSM-5, most preferred of which have SiO₂/Al₂O₃ mole ratios of greater than about 25, and mordenite, and beta zeolite, and combinations of these. Depending on the silica/alumina ratio, zeolites can have mainly physical adsorption or a combination of physical and chemical adsorption. In physical adsorption, the adsorbents weakly hold the adsorbed species within or on their structure. Species that are physically adsorbed, desorb at relatively low temperatures, eg., room temperature. In chemical adsorption, the adsorbents strongly hold the adsorbed species within their structure. Species that are chemically adsorbed, desorb at relatively high temperatures ie, typically above room temperature. (Low and high temperatures are strictly relative terms). As is known in the art, a zeolite can function also as a cracking catalyst or an oxidation catalyst. For oxidation, the zeolite can have a catalyst metal exchanged therein. A zeolite can be used as formed or ammoniated, but is preferably in the H⁺ form, or ion exchanged with an alkali or alkaline earth metal, but preferably with a transition metal e.g., of atomic number 21 thru 79, as a noble metal, e.g., Pt or Pd, etc., as is known in the art depending on the adsorption or conversions which are desired. Some drying agent-adsorbing agent combinations that are suited to the practice of the present invention are as follows: Drying Agent Adsorbing Agent KA or NaA or K-Erionite ZSM-5 Gamma alumina ZSM-5 Silica gel ZSM-5 KA or Clinoptilolite or gamma alumina USY 13X or Phillipsite or silica gel Beta Chabazite or NaA USY + mordenite KA or Phillipsite ZSM-5 + USY + mordenite NaA or Chabazite Beta + USY The drying agent and hydrocarbon removing agents can be used in any form. For example they can be typically in contact with substrates. The substrates can be of any size and shape suitable to the application, for example, pellets, beads, monoliths, etc. The substrates are most typically monolith substrates. The monoliths are typically bodies having inlet and outlet ends and a multiplicity of open ended cells extending from inlet to outlet end with porous walls between and separating adjacent cells from one another. The monoliths are preferably honeycomb structures. The drying agent and hydrocarbon-removing agent can be applied to the substrate by conventional washcoating or spraying techniques. For example, the substrate is contacted with a slurry containing the agent and other components such as binders, and dispersing agents, etc, as is known in the art. Some binders are aluminum oxide, most preferred of which is the precursor boehmite, other precursors of aluminum oxide, e.g., aluminum nitrate, and silica, titania, zirconia, rare earth oxides, e.g., ceria, etc, and their precursors. Some typical compositions that can be used for drying agents and hydrocarbon-removing agents are in percent by weight 0 to about 50 methylcellulose, 0 to about 50 silica, 0 to about 50 Al₂O₃ from boehmite, aluminum nitrate, or alumina sol, and about 50 to about 95 of the agent. More preferred compositions are in percent by weight 0 to about 5 methylcellulose, 0 to about 10 silica, 0 to about 15 alumina from aluminum nitrate, 0 to about 15 alumina from boehmite, and about 70 to about 90 being the agent. Unavoidable impurities can also be present in the compositions of the present invention, if they do not interact with the constituents of these compositions. However, impurities that cause sintering or destruction of the zeolite structure must be kept at low levels. Most typically, impurities should be kept below about 5 wt.%, preferably below about 1% and most preferably below about 0.01%. Some especially preferred compositions for the drying agent are given in Table 1, and for the hydrocarbon-removing agent, in Table 2. In each case, the constituents or their precursors are blended with about 0.5 to about 2.0% methylcellulose (Dow A4M). In each case a slurry is formed in a suitable machine such as a ball mill, mix-muller, or double-arm mixer by admixing with a liquid medium optionally containing about 0.01 to about 1.0% by weight surface active agent such as Airco's Surfanol 485. The preferred liquid medium is water, however organic liquids in combination with water can also be used, for example, isopropyl alcohol + water. Organic liquids by themselves can also be used, e.g., toluene or xylene. Weight Percent Constituents Of Drying Agent Compositions After Final Heat Treatment Dryer Constituent A B C D E NaA zeolite - - - - - KA zeolite 85 85 - - - Type X zeolite - - 85 - - Gamma alumina - - - 85 - Silica gel - - - - 85 Gamma alumina [from Dispersal Boehmite, Condea Chemie] - 5 12 15 - Gamma alumina [from Nyacol Al colloidal alumina sol] 15 10 - - - Gamma alumina [from Reagent Aluminum Nitrate] - - 3 - - Silica [from DUPONT Ludox HS-40] 15 Dryer Constituent F G H I J NaA zeolite 45 - - 80 - KA zeolite - 45 - - - Type X zeolite - - 45 - - Gamma alumina 45 - - - - Silica gel - 45 45 - 90 Gamma alumina [from Dispersal Boehmite, Condea Chemie] - - - 17 10 Gamma alumina [from Nyacol Al colloidal alumina sol] 15 - 10 - - Gamma alumina [from Reagent Aluminum Nitrate] - - - 3 - Silica [from DUPONT Ludox HS-40] - 10 - - - These compositions in slurry form are used to coat monolith substrates. For example, the substrate is dipped into the slurry, repeatedly if necessary until the desired amount of the composition is coated on the substrate. Excess slurry is removed and the coated substrate is dried and fired. Another technique of applying the agents to the substrates is to fill the cells of the multicellular substrate with the agent. In this technique, a paste is formed of the agent, binder or binders, and plasticizers. A preferred binder and plasticizer is methylcellulose. A vehicle is used to attain the proper plasticity, viscosity for handling and filling. For example, the constituents in Table 1 or 2 can be used with a suitable amount of liquid medium to form the paste. The paste is formed in a suitable machine such as a mix-muller, double-arm mixer, or calender rolls by admixing the constituents with a vehicle. The preferred vehicle is water, however, organic liquids in combination with water can be used, for example, isopropyl alcohol and water. Or organic liquids alone can be used, e.g., toluene or xylene. The paste is injected into selected cells of the substrate such as by hydraulic injection e.g., using a hydraulic press. One especially preferred technique for loading honeycombs with the agent containing material is to use bodies which have alternate cells plugged at one end. In this technique, the cells or channels which are not to be filled are plugged at one end. This can be done by any known technique. In one technique a mask usually of rubber, is used. The mask has openings to match the cell number and size of the cells of the body. One set of openings is blocked by the rubber mask in the pattern that is contemplated for the cells which are to be subsequently loaded. The mask is placed on one end of the body and the cells of the body not blocked by the mask are plugged with plugging material. The plugging material is typically a low firing ceramic composition but can be any type of cementicious or polymer type material which after heat treatment or curing is inert to the filling operation. The mask is then removed and the body is heat treated or cured and is then ready to be loaded with filler material. One preferred technique for loading the cells of the body is to introduce a mixture of the desired composition of filler material which is typically in the form of a paste, into the end of the body which has plugged cells exposed to the paste. Filling of the cells is accomplished by pushing the appropriate amount of paste material into the unplugged cells with a hydraulic press. If necessary, the loaded body is then dried and fired to remove liquid phases, fugitive additions such as temporary binders and rheological agents. The plugging is then removed, such as by sawing it off. If polymers are used as the plugging material, the plugs are burned off. The substrates are made of material that is suitable preferably for high temperature applications. Some preferred materials are those that include as a predominant phase: ceramic, glass-ceramic, glass, high surface area-high temperature stable oxides, metals, and combinations thereof. By combinations is meant physical or chemical combinations, eg., mixtures, compounds, or composites. Some materials that are especially suited to the practice of the present invention, although it is to be understood that the invention is not limited to these, are those made of cordierite, mullite, clay, talc, zircon, zirconia, spinel, alumina, silica, borides, lithium aluminosilicates, alumina silica, feldspar, titania, fused silica, nitrides, borides, carbides, eg., silicon carbide, silicon nitride or mixtures of these. Some typical ceramic substrates are disclosed in U.S. Patents 4,127,691 and 3,885,977. Those patents are herein incorporated by reference as filed. Other types of bodies are porous metal bodies. Some preferred types of porous metal bodies, although it is to be understood that the invention is not limited to such, are bodies made of iron group metals such as, for example, Fe-Al or Fe-Cr-Al with optional additions for enhancement of various properties. For example, additions of oxides are included for enhancement of properties such as heat, corrosion, oxidation resistance, etc. Some porous metal bodies which are especially suited to the practice of the present invention are discussed in U.S. patents 4,758,272 and 4,992,233 and in U.S. application No. 07/767,889, filed September 30, 1991 corresponding to EP-A-0 488 716. These patents and application are herein incorporated by reference as filed. Some examples of honeycombs produced by the process of the present invention, although it is to be understood that the invention is not limited to these, are those having about 94 cells/cm² (about 600 cells/in²), about 62 cells/cm² (about 400 cells/in²), or about 47 cells/cm² (about 300 cells/in²), those having about 31 cells/cm² (about 200 cells/in²), or about 15 cells/cm² (about 100 cells/in²), or about 2.5 cells/cm², (about 16 cells/in²) or about 1.5 cells/cm² (about 9 cells/in²). These bodies are made preferably of, but not limited to materials which when fired form cordierite. Typical wall thicknesses in catalytic converter applications, for example, are about 6 mils (about 0.15 to about 0.6 mm). The external size and shape of the body is controlled by the application, e.g., engine size and space available for mounting. The substrate body can have any degree of wall porosity from essentially none, or low to high. For example, typically the wall porosity ranges from 0% by volume to higher values which are determined by practical limits depending on the composition of the substrate and the intended application, e.g., the nature of the material which is to be coated on the walls, etc. The porosity is typically about 30% to about 70% by volume. The invention is especially suited for low-to-moderate porosity bodies, that is, those having total porosities of about 30% to about 50% by volume. In general, the average pore size is about 2 to about 70 and preferably about 3 to about 50 microns in diameter for most applications. The compositions of Tables 1 and 2 can be formed into bodies such as extruded monoliths by methods known in the art, for example, silica gel drying agent, alumina drying agent, and mordenite hydrocarbon-removing agent. Silica gel can be formed in situ by reaction of sulfuric acid with sodium silicate, etc. or the already formed silica gel powder can be extruded. This is done typically by mixing raw material powders, inorganic and organic additives and binders, plasticizing with water, forming into a body such as by extruding, e.g., a honeycomb, drying and firing at about 400°C to about 800°C. A most preferred technique is given in the examples that follow. The alumina monolith can be formed from a plasticizable mixture of an alumina precursor such as boehmite. The hydrophilic material is located upstream from the hydrocarbon removing agent. The drying agent and the hydrocarbon removing agent can share one substrate unit in which case the hydrophilic material is on the inlet end of the substrate and the hydrocarbon removing agent is on the outlet end. Or they can be on separate units or they themselves can form separate units, or there can be any combination of these. Additionally, hydrophilic material can be located downstream of the hydrocarbon adsorbing agent. This prevents moisture from back diffusing through the exhaust system and reaching the hydrocarbon adsorbing agent especially after the engine has been shut down. In auto exhaust conversion applications, the drying agent and hydrocarbon removing agent can be used in any conventional form. The agents are typically on substrates which are placed one after the other so the exhaust gas flows from inlet to outlet ends sequentially from one to the other. Although it is not necessary, by-pass valving can be used as is known in the art to first direct exhaust gas flow to the drying agent and hydrocarbon-removing agent system, and then to the main body catalyst. After adsorption, the system is by-passed and after normal engine operating conditions are attained and the main catalyst is functioning, the system can be desorbed. The system can then be by-passed until the next start-up period. The desorption cycle is that in which the adsorbed water desorbs and passes out of the system, and the adsorbed hydrocarbons desorb and are either recirculated to the engine, or converted by the main body catalyst and exit the system as CO₂ and water. The main body catalyst, that is, the catalyst for converting NO x , CO, and hydrocarbons to innocuous products can be any conventional catalyst known in the art. By innocuous products is meant those that are generally considered to be harmless to health and the environment, such as CO₂, N₂, H₂, and water. Some preferred main body catalysts are for example, noble metal as eg, Pt, Pd, Rh, or combinations thereof on alumina, ceria, lanthana, zirconia, yttria, or combinations thereof. It is especially preferred to use a three-way catalyst. Some typical three-way catalysts which are especially suited to the practice of the present invention for auto exhaust conversion are Pt on ceria-alumina combined with Rh on zirconia. The Pt-ceria-alumina and the Rh-zirconia can be combined and applied at once, as in a single coating or they can be applied in separate coatings. Another suitable catalyst is Pt/Pd/Rh on gamma alumina with a rare earth oxide such as ceria. In auto exhaust conversion applications, the substrates (or agents which are in the form of monolith structures) are held fixed in conventional canisters by conventional means such as, for example, by metal mesh, or ceramic mats, etc. Refractory fibrous material is often used to prevent passage of gases between the stages and the canister. To more fully illustrate the invention, the following non-limiting examples are presented. All parts, portions, and percentages are on a weight basis unless otherwise stated. Preparation of adsorbing agents and drying agents which are used in the following Examples Preparation of hydrocarbon adsorber Weighed quantities of ZSM-5 zeolite (silica/alumina = 26:1) and colloidal gamma alumina binder are mixed into deionised water and then roll milled for about 2 hours to obtain a uniform dispersion containing about 85% zeolite and 15% gamma alumina on a dry weight basis. About 0.5% Surfanol 485 by Airco is used to assist dispersion and to function as a wetting agent. A cordierite honeycomb substrate (5.15g, about 400 cells/in², or about 47 cells/cm², 1" (2.54 cm) diameter, 1" (2.54 cm) length) is then dipped into the dispersion for about 1 minute, removed, and the channels blown out with a stream of air to remove excess liquid. The coated substrate is then dried at about 150°C in a circulating air oven and weighed. If insufficient coated solids are present, the dipping and drying procedure is repeated until the desired weight of coating is obtained. The substrate with the coating is then fired at about 500°C for about 3 hours, and weighed. This sample weighs about 7.34 g (about 5.06 g cordierite, about 1.94 g zeolite + 0.34 g alumina binder). Preparation of alumina drying agent honeycombs Composition: About 90 parts Vista Catapal boehmite, 12.2 micron average particle size, about 5 parts Cabosil EH-5 silica, about 6 parts Dow Chemical methylcellulose grade K75 about 50 parts of Remet Dispural slurry of about 89% distilled water, about 10% Dispural Boehmite, about 1% acetic acid, adjusted to pH about 3.3 with ammonia, and aged overnight and pH adjusted to about 7.0, about 20 parts distilled water. Fabrication of honeycombs The above first three constituents are dry mixed in a laboratory Brabender intensive mixer. They are then combined with the last two constituents in a laboratory mix-muller and thoroughly plasticized. One inch (about 2.54 cm) diameter honeycombs are extruded of about 400 cells/in²), or about 47 cells/cm², about 0.006" (about 0.15 mm) wall thickness. These are dried at about 100°C and then fired at about 500°C for about 6 hours. The honeycombs each contain about 3.7 g of gamma alumina. Preparation of Type KA zeolite drying agent Composition A of Table 1 is prepared by mixing KA zeolite powder and colloidal gamma alumina binder in deionized water. This mixture is then roll milled for about 2 hours to obtain a uniform dispersion containing about 85% zeolite and about 15% gamma alumina binder on a dry weight basis. About 0.5% Surfanol 485 by Airco is used to assist dispersion and as a wetting agent. The weighed cordierite honeycomb substrate (5.26 g about 400 cells/in², or about 47 cells/cm², 1" (2.54 cm) diameter, 1" (2.54 cm) length) is then dipped into the dispersion for about 1 minute, removed, and the channels blown out with a stream of air to remove excess liquid. The coated substrate is then dried at about 100°C in a circulating air oven and weighed. If insufficient coated solids are present, the dipping and drying procedures are repeated until the desired weight of coating is obtained. The substrate with the coating is then fired at about 500°C for about 3 hours and weighs about 7.3 g total (1.73 g type KA zeolite, 0.31 g binder.) Preparation of silica gel drying agent The following mixture is made up: 18% silica gel supplied by WR Grace, grade 81, reduced to a powder of about 10 microns average particle size, 65% CE Minerals fused quartz grade 44I, (-325 mesh), 17% Dow Corning silicone resin Q6-2230 and 6% methylcellulose [F-60 DOW Methocel] (all percents are on a dry weight basis). To this mixture is added about 36% of a liquid containing a 50:50 mixture of water + isopropyl alcohol. The liquid and solid mixture is plasticized in a mix-muller, and then extruded using conventional means, into a honeycomb monolith having about 400 cells/in², or about 47 cells/cm². It is dried and fired at about 500°C for about 6 hours. The 1" (2.54 cm) diameter x 1" (2.54 cm) length honeycomb contains about 1.5 g of silica gel drying agent. The hydrocarbon containing gas stream used in the following examples has the following composition (vol%): NO x = 1000 ppm, CO = 1%, H₂ = 0.33%, O₂ = 0.77%, CO₂ = 14%, propylene = 500 ppm, 2.5% water, balance N₂. Space velocity = 50,000 volume changes/hr Example 1 (Illustrative) To experimentally show the working of this invention, the following was done. The honeycomb that is coated with the Type KA zeolite drying agent (Composition A of Table 1) is placed in the upstream position in a test furnace and the honeycomb with the ZSM-5 zeolite hydrocarbon adsorber (Composition J of Table 2) is placed in the downstream position. The samples which have the composition given above, are exposed to the synthetic exhaust gases over the temperature range ambient to about 600°C, and then cooled. This activates the drying agent as well as the hydrocarbon adsorbing agent, because no water was present. The experiment is then repeated with about 2.5 vol. % water added to the above synthetic exhaust gas mixture. Example 2 (Illustrative) The procedure of Example 1 is repeated except that the drying agent is the extruded silica gel (instead of the 3A zeolite), which is placed upstream of the ZSM-5 zeolite adsorber. Example 3 (Illustrative) The procedure of Example 1 is repeated except that the drying agent is the gamma alumina honeycomb (instead of the KA (3A) zeolite), which is placed upstream of the ZSM-5 zeolite adsorber. Example 4 (Comparative Control) The procedure of Example 1 is run except that there is no upstream drying agent present. The Figure is plotted as the quantity of adsorbed propylene (in mg) against time (in min.) up to about 5 minutes for the four examples. This time is sufficient since engine cold start period is essentially in the initial 2-3 minutes. The lower curve shows the adsorption of propylene on the ZSM-5 zeolite (Example 4, comparison control run) when no drying agent is present. Only about 4-5 mg of propylene are adsorbed during the initial 5 minutes. With the type 3A zeolite, silica gel, and gamma alumina drying agents, it is seen that a substantially larger amount of propylene adsorption occurs during the first several minutes than when no drying agent is used. These data show that the drying agent in the system eliminates the poisoning effect of water during the first few minutes of exposure to the wet exhaust gases.

Claims: A method for removing hydrocarbons from a gaseous mixture which comprises water and hydrocarbons, the method comprising: a) contacting the mixture with hydrophilic material to remove at least some of the water therefrom and produce a dried mixture; and thereafter b) contacting the dried mixture with an agent for removing hydrocarbons, to produce a purified mixture. A method of claim 1 wherein the hydrophilic material is at least one selected from molecular sieve wherein the pores defined by the crystalline structure of said molecular sieve are large enough for adsorption of water molecules, high surface area aluminas, precursors for high surface area aluminas, and high surface area silicas. A method of claim 2 wherein the molecular sieves have a pore size greater than about 0.2 nm (2 angstroms) in diameter. A method according to claim 3 wherein the molecular sieves have a pore size of about 0.2 to about 0.5 nm (about 2 to about 5 angstroms) in diameter. A method of claim 2 wherein said molecular sieve is at least one kind selected from Type A zeolite, Type L zeolite, Type X zeolite, chabazite, erionite, clinoptilolite, ferrierite, phillipsite, mazzite, offretite, aluminophosphates, and silicoaluminophospates, or NaA zeolite, CaA zeolite, KA zeolite, LiA zeolite, NaX zeolite, K-erionite, phillipsite. A method of claim 2 wherein the surface are of said aluminas and said silicas is selected from the group comprising an area of at least about 200 m²/g, or at least about 300 m²/g. A method of any one of claims 1-6 wherein the hydrophilic material is silica gel or gamma alumina. A method of any one of claims 1-7 wherein the hydrocarbon-removing agent comprises at least one molecular sieve. A method of claim 8 wherein said molecular sieve is selected from the group consisting of zeolite, carbon molecular sieve, metallophospates, aluminophosphates, silicoaluminophosphates, of pentasil type zeolite, faujastie type zeolite, mordenite zeolite, beta zeolite, or ultra stable Y zeolite, ZSM type zeolite, or combinations of any of the foregoing group members. A method of any one of the foregoing claims wherein the hydrocarbons are alkanes and alkenes with 1 to 6 carbon atoms. An apparatus for removing hydrocarbons from an exhaust gas mixture which comprises water and hydrocarbons, the system comprising: a) a first stage comprising hydrophilic material for removing at least some of the water from the mixture to produce a dried gas mixture; and b) a second stage comprising a hydrocarbon-removing agent for removing hydrocarbons from the dried mixture, to produce a purified mixture. An apparatus of claim 11 further comprising a third stage which comprises hydrophilic material for removing excess water from the system, the third stage being positioned downstream of the hydrocarbon-removing agent. An apparatus of claim 11 or 12 further comprising a catalyst for removing NO x , CO, and hydrocarbons, said catalyst being positioned downstream of the hydrocarbon-removing agent.

Inventors: HERTL WILLIAM, LACHMAN IRWIN MORRIS, HERTL, WILLIAM, LACHMAN, IRWIN MORRIS
Applicants: CORNING INC, CORNING INCORPORATED
Application year: 1993
Main classification: B01D53
IPC codes: B01D53, B01J37