Patent Application
20050002843
This application claims priority under 35 U.S.C. § 119 or 365 to Republic of Korea Patent Application Nos. 10-2003-0028926, filed May 7, 2003, and 10-2004-0020956, filed Mar. 27, 2004. The entire teachings of these Korean Patent Applications are incorporated herein by reference.
Generally, the present invention relates to a method of treating nitrogen oxides (NOx) contained in an exhaust gas from a combustion process of a stationary source and a mobile source using gases and liquid oils as fuels, such as gasoline, kerosene and bio-diesel oil. Particularly, the present invention relates to an apparatus and a method of treating nitrogen oxides where an alumina-promoted silver catalyst is installed in a flow path of the exhaust gas and a reducing agent is sprayed into the exhaust gas passing through the catalyst.
As well known to those skilled in the art, a composition of nitrogen compounds contained in a combustion exhaust gas varies, sensitively depending on the type of fuel and operational conditions of an engine. A selective catalytic reduction (SCR) process is a conventional process used for removing nitrogen oxides, in which nitrogen oxides are broken down into nitrogen and water by a reaction with a reducing agent in the presence of a catalyst. Ammonia is widely used as the reducing agent in the selective catalytic reduction process, because it has excellent catalytic reactivity and selectivity.
For example, U.S. Pat. No. 5,024,981 discloses an NH3-SCR process for selectively removing nitrogen oxides contained in the exhaust gas with a honeycomb-structured catalyst, in which an active material, comprising vanadium or tungsten, is supported by a titania carrier.
However, ammonia is a very toxic gas, and the allowable limit of ammonia is significantly lower (5 ppm or lower) than that of nitrogen oxides. Thus, leakage of ammonia can cause serious environmental pollution. For this reason, practically, after the amount of nitrogen oxides contained in the exhaust gas is measured by an analyzer, a corresponding ammonia amount is sprayed into the exhaust gas to reduce nitrogen oxides. However, it is difficult to effectively reduce nitrogen oxides if the concentration of nitrogen oxides varies. Also, in the case of spraying ammonia into the exhaust gas after the amount of nitrogen oxides is analyzed, an undesirable time lag occurs, causing an ammonia-slip phenomenon in which nitrogen oxides and unused ammonia pass through a catalytic bed without reacting with each other. The molar ratio of ammonia to nitrogen oxides may be controlled to be 1 or lower to minimize the ammonia-slip phenomenon. However, control of the molar ratio of ammonia to nitrogen oxides still cannot overcome the above mentioned disadvantages.
In accordance with a recent trend of large-sized buildings and amusement facilities, an independent electric power plant for a stable electricity supply is installed in the buildings and amusement facilities. Ammonia may be used as the reducing agent to reduce nitrogen oxides discharged from the independent electric power plant. However, use of ammonia is strictly limited because of potential large-scaled accidents due to the leakage of ammonia, which can lead to serious environmental pollution.
To overcome the disadvantages of the NH3-SCR process, an HC-SCR (hydrocarbon SCR) process recently has been started to be used, in which hydrocarbons is used as a reducing agent. For example, an HC-SCR process using propane as the reducing agent is discussed in U.S. Pat. No. 5,993,764. However, the process has not been commercialized yet because of its low removal activity of nitrogen oxides. U.S. Pat. Nos. 5,824,621 and 6,284,211 B1 discuss an ethanol-SCR process for converting nitrogen oxides into nitrogen using ethanol as a reducing agent in the presence of a silver catalyst, which is being commercialized. Generally ethanol has a relatively high removal effect of nitrogen oxides in comparison with other hydrocarbon-based reducing agents.
The present invention has been made, keeping in mind the above problems in the prior art. An object of the present invention is to provide a catalyst for reducing nitrogen oxides contained in an exhaust gas from a combustion process of a stationary source and/or a mobile source.
Another object of the present invention is to provide an apparatus for removing nitrogen oxides contained in an exhaust gas from a combustion process of a stationary source and mobile source, in which a reducing agent is injected into the exhaust gas passing through an alumina-promoted silver catalyst installed in the flow path of the exhaust gas.
It is still another object of the present invention to provide a method of removing nitrogen oxides contained in an exhaust gas from a combustion process of a stationary and/or a a mobile source.
In order to accomplish the above objects, the present invention provides an alumina-promoted silver catalyst for removing nitrogen oxides.
Further, the present invention provides an apparatus for treating nitrogen oxides that includes an inlet pipe to receive the exhaust gas. A reactor includes one or more nozzles connected to the inlet pipe to spray air and a reducing agent to the exhaust gas passing into the reactor through the inlet pipe. The reactor also includes at least one catalytic bed installed behind the nozzle to reduce nitrogen oxides from the exhaust gas laden with the reducing agent. A storage tank stores therein the reducing agent to be sprayed by the nozzle. An injection pump is installed between the storage tank and the nozzle to transport the reducing agent from the storage tank to the nozzle. Additionally, an air pump is connected to the nozzle to feed air into the nozzle. An outlet pipe discharges the exhaust gas that has gone through the catalytic bed.
Furthermore, the present invention provides a method of treating exhaust gas, including the steps of injecting a reducing agent into the exhaust gas containing nitrogen oxides from a combustion process of a stationary source or a mobile source and of passing the treated exhaust gas with the reducing agent through a catalytic bed to reduce nitrogen oxides contained in the exhaust gas.
Nitrogen oxides (NOx) in the present invention means compounds such as NO, NO2, N2O5 and N2O. The term “nitrogen oxides” is used to describe one or more of NO, NO2, N2O5, N2O and other oxides of nitrogen. It is understood that the word “reducing” as used herein is to reduce nitrogen oxides contained in the exhaust gas, and generally has the same meaning as removing nitrogen oxides.
The objects, features and advantages of the present invention will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings, in which:
According to the present invention, a catalyst for reducing nitrogen oxides comprises silver and alumina(Ag/Al2O3). The catalyst can be further treated by sulfuric acid. The catalyst further treated by sulfuric acid includes sulfates, and exists in the form of Ag/Al2O3—SO42−.
It is preferable that an alumina carrier has an amorphous, gamma-type, theta-type, or eta-type crystalline structure in order to reduce nitrogen oxides easily. For use in a catalyst, the alumina carrier that has various crystalline structures, as described above, is coated on a honeycomb body, and preferably on a cordierite honeycomb body. Additionally, the content of the alumina carrier in the catalyst is preferably 0.05 to 0.3 g/cm3 based on the whole catalyst. If the content of the alumina carrier is less than 0.05 g/cm3, catalytic activity is greatly reduced. The catalytic activity increases as the content increases up to 0.3 g/cm3. When the content is more than 0.3 g/cm3, the catalytic activity no longer increases.
A “catalytic bed” designates a honeycomb body coated with the catalyst, and installed in the apparatus for treating nitrogen oxides.
In the present invention, silver is provided in a form of reduced silver (Ag°), silver oxide (AgO), silver chloride (AgCl), silver nitrate (AgNO3), silver sulfate (Ag2SO4), or a mixture thereof. The amount of silver is preferably 1 to 10 wt % based on the alumina carrier. If the amount of silver is less than 1 wt %, catalytic activity is greatly reduced. On the other hand, if the amount of silver is greater than 10 wt %, the catalytic activity no longer increases.
According to the present invention, the catalyst for removing nitrogen oxides optionally can be placed in a 0.01 to 1 M sulfuric acid aqueous solution to treat the catalyst with sulfuric acid. In this case, the catalyst exists in the form of Ag/Al2O3—SO42−.
When the alumina-promoted silver catalyst is used to reduce nitrogen oxides after being placed in a 0.01 to 1M sulfuric acid aqueous solution, removal activity of nitrogen oxides of the resulting catalyst is greatly improved at a predetermined temperature range. For example, at a temperature of 250 to 500° C., poisoning resistance of the catalyst to sulfur dioxide is improved.
Alternatively, instead of placing the catalyst in a sulfuric acid aqueous solution, sulfur dioxide may be continuously injected into the alumina-promoted silver catalyst to treat the catalyst with sulfuric acid. The sulfuric acid-treated catalyst using sulfur dioxide has similar catalytic activity to that of the sulfuric acid-treated catalyst using a sulfuric acid aqueous solution.
In the present invention, the term “sulfuric acid-treated” means that the catalyst is placed in a sulfuric acid aqueous solution, or continuously injected by sulfur dioxide.
Also, it should be understood that the word “catalyst” as used herein is intended to include not only the alumina-promoted silver catalyst, but also the honeycomb body on which silver is coated.
Hereinafter, a description of a method of producing the catalyst for reducing nitrogen oxides according to the present invention will be given. In a preferred embodiment, the catalyst of the present invention is coated on the honeycomb body, and the method of producing the catalyst coated on the honeycomb body is described herein.
The method of producing the catalyst according to the present invention includes the steps of slowly adding alumina to ion-exchanged water with strong agitation to produce a homogeneous slurry; coating such slurry on the honeycomb body, preferably on the cordierite honeycomb body, more preferably on the cordierite honeycomb body with a size of about 15×15×10 cm and a cell density of about 200 cells/in2 (84×84 cells); firstly drying the coated honeycomb body at room temperature for about 24 hours; drying the firstly dried honeycomb body at about 120° C. for about 4 hours, heating the dried honeycomb body at a rate of about 10° C./min to 500 to 700° C. and calcining the heated honeycomb body at 500 to 700° C. for about 2 hours; drying the calcined honeycomb body at room temperature for about 24 hours after placing the calcined honeycomb body in a silver-containing solution, such as silver chloride (AgCl), silver nitrate (AgNO3), silver sulfate (Ag2SO4), or a mixture thereof; drying at about 120° C. for about 4 hours the honeycomb body placed in the silver-containing solution and then heating the honeycomb body at a rate of about 10° C./min to 500 to 700° C.; and calcining again the honeycomb body at 500 to 700° C. for about 2 hours.
In the present invention, the catalyst for removing nitrogen oxides optionally is placed in an acid solution, such as a 0.01 to 1 M sulfuric acid aqueous solution, and then dried at room temperature for about 24 hours. The next step is to further dry the catalyst at about 120° C. for about 4 hours, then heat at a rate of about 10° C./min to 500 to 700° C., and finally, calcine at 500 to 700° C. for about 2 hours, thereby accomplishing the sulfuric acid-treated catalyst according to the present invention.
In the apparatus for treating nitrogen oxides according to the present invention, the exhaust gas, discharged from a combustion process of a stationary source and/or a mobile source, preferably a combustion process of a stationary source and/or a mobile source using gases or gasoline as a fuel, contains a lower content of sulfur oxides, such as sulfur dioxide, than does the exhaust gas from a combustion process of a stationary source and/or a mobile source using coals as a fuel.
A reducing agent according to the present invention is sprayed into the exhaust gas with air through the nozzle to reduce nitrogen oxides contained in the exhaust gas into nitrogen and water. The molar ratio of the reducing agent to nitrogen oxides contained in the exhaust gas is at least 0.1 or above.
The reducing agent for reducing nitrogen oxides to nitrogen may be any substance, including hydrocarbons, such as unsaturated hydrocarbon, heterogeneous hydrocarbon and preferably, ethanol.
Air allows the reducing agent to be widely sprayed from the nozzles into the exhaust gas. Any gas can be used instead of air as long as it is inert and does not react with the reducing agent. However, it is preferable that air is used in conjunction with the reducing agent in consideration of its price and ease in obtaining it.
Reference should now be made to the drawings, in which the same numbers are referred to throughout the different drawings to designate the same or similar components.
With reference to
The reactor 4 is defined as a space in which the nozzles 8 and catalytic beds 10 are installed to reduce nitrogen oxides contained in the exhaust gas.
The nozzles 8 and catalytic beds 10 are installed in the reactor 4 in such a way that a tube, including the nozzles 8, is positioned at the front of each catalytic bed 10 based on a flow direction of the exhaust gas. In the case of installing one or more tubes and catalytic beds 10 in the reactor 4, the tube pairs with a catalytic bed 10, and the tube and catalytic bed 10 are alternately positioned in the reactor 4.
The inlet pipe 2, according to the present invention, is connected to the stationary or mobile source at the beginning part thereof to receive the exhaust gas containing nitrogen oxides from the combustion process of the stationary or mobile source, and sequentially is connected to the reactor 4 and the outlet pipe 6 at the ending part thereof to reduce nitrogen oxides contained in the exhaust gas and discharge the treated exhaust gas through the outlet pipe.
The nozzles 8 according to the present invention are installed in the reactor 4 to spray air and the reducing agent to the exhaust gas containing nitrogen oxides that passes through the reactor 4. The nozzles 8 may be installed in any manner in the reactor 4 so long as air and the reducing agent are desirably sprayed into the exhaust gas. Preferably, the nozzles 8 can be installed in the reactor 4 in a single- or multi-injection manner to easily spray air and the reducing agent into the exhaust gas containing nitrogen oxides at 200 to 500° C. through the reactor 4.
It is called a single-injection manner when a single tube 18 is structured such that a plurality of holes is formed on a surface of the tube 18 and the nozzles 8 are connected to the holes. In a multi-injection manner, two or more tubes are installed in the reactor 4, as described above.
According to the multi-stage injection manner, when a hydrocarbon-based reducing agent, such as ethanol, is injected into the reactor 4, it is judged against the amount of the sprayed reducing agent whether the amount of the reducing agent consumed during the reduction of nitrogen oxides is proper or not. Thus, the multi-stage injection manner has higher removal activity of nitrogen oxides than that of the single-stage injection manner at the same amount of the reducing agent as used in the multi-stage injection manner.
The apparatus for treating nitrogen oxides according to the present invention may optionally further comprise valves 22 installed in the tubes 18 to control the flow rate of a fluid passing through each of the tubes 18. One or more concentration sensors 24 are installed in the inlet pipe 2, the reactor 4, or the outlet pipe 6 to sense the concentration of nitrogen oxides that exist in the exhaust gas flowing through the inlet pipe 2, the reactor 4 and the outlet pipe 6. A control unit 20 connected to the valves 22 and concentration sensors 24 to control the valves 22 based on concentration data from the concentration sensors 24 may also be installed.
In the present invention, the concentration sensors 24 can be installed at any position in the inlet pipe 2, the reactor 4 and the outlet pipe 6 so long as the concentration of the exhaust gas flowing in the inlet pipe 2, the reactor 4, and the outlet pipe 6 are easily measured.
The nozzles 8 and an outer surface of each of the tubes 18 connected to the nozzles 8 may optionally be insulated by an insulating material to prevent the exhaust gas at 200 to 500° C. from combusting the reducing agent. Additionally, cool air may be fed through the nozzles 8 and/or tubes 18 that are covered by an insulating material to effectively prevent the reducing agent passing through the nozzles 8 and the tubes 18 from being combusted by the high temperature of the exhaust gas.
As described above, the nozzles 8 that function to spray air and the reducing agent are connected to the air pump 16 that compresses air supplied from the atmosphere. The nozzles 8 are also sequentially connected to the injection pump 12 that feeds the reducing agent to the nozzles 8, and the storage tank 14 that stores the reducing agent therein. The injection pump 12 acts as a power source to feed the reducing agent from the storage tank 14 to the nozzles 8.
In the present invention, the air pump 16 supplies the compressed air with the reducing agent into the nozzles 8. The air pump 16 allows injecting the reducing agent at a high pressure into the reactor 4, thereby the exhaust gas containing nitrogen oxides and the reducing agent are readily mixed.
Hereinafter, a preferred operation mode of the apparatus according to the present invention will be described.
The exhaust gas containing nitrogen oxides from the combustion process of the stationary source and mobile source using gas or liquid oil, such as gasoline, kerosene or bio-diesel oil as fuel is fed through the inlet pipe 2 into the reactor 4 which includes the nozzles 8 and catalytic beds 10.
The reducing agent stored in the storage tank 14 is then fed into the nozzles 8 by the injection pump 12, and air is simultaneously fed into the nozzles 8 by air the pump 16.
Additionally, air and the reducing agent fed into the nozzles 8 positioned in the reactor 4 are sprayed into the exhaust gas containing nitrogen oxides passing through the reactor 4.
Further, the exhaust gas mixed with the reducing agent passes through the catalytic beds 10 positioned behind the nozzles 8 to reduce nitrogen oxides contained in the exhaust gas to nitrogen.
Furthermore, the treated exhaust gas is discharged through the outlet pipe 6 connected to the ending part of the reactor 4.
Compressed air from the air pump 16 is fed in conjunction with the reducing agent into the nozzles 8, which allows spraying the reducing agent at a high pressure into the exhaust gas so that the exhaust gas containing nitrogen oxides and the reducing agent are readily mixed.
The apparatus for treating the exhaust gas according to the present invention may include the concentration sensors 24 for sensing a concentration of nitrogen oxides contained in the exhaust gas, and can effectively treat the exhaust gas using the control unit 20 that controls the valves 22 based on the concentration data measured by the concentration sensors 24.
As described above, the apparatus is structured such that one or more tubes 18, each including a plurality of nozzles 8, are installed in the reactor 4, each of the tube 18 is connected to the injection pump 12 and air pump 16 and at least one concentration sensor 24 is installed in the inlet pipe 2, the reactor 4 and the outlet pipe 6.
The valves 22 that control the degree of opening and closing of the tubes are installed in the tubes 18. The valves 22 and concentration sensors 24 are connected to the control unit 20.
When the exhaust gas containing nitrogen oxides is discharged from the combustion process of the stationary source and mobile source using gases or liquid oil as a fuel, such as gasoline, kerosene or bio-diesel oil, the exhaust gas is fed into the reactor 4 past the tubes 18, each including a plurality of nozzles 8.
In the present invention, the concentration of nitrogen oxides contained in the exhaust gas is measured by the concentration sensors 24 installed in the inlet pipe 2, the reactor 4 and the outlet pipe 6, which can transmit the concentration data to the control unit 20.
After a removal activity rate of nitrogen oxides by the catalytic beds 10 is estimated based on the concentration data output from the concentration sensors 24, the control unit 20 opens the valve 22 of a tube 18 positioned at the front of the catalytic bed 10 poisoned by the reaction of the exhaust gas and the reducing agent, while closeing the valve 22 of another tube 18 positioned at the front of the non-poisoned catalytic bed 10.
The reducing agent stored in the storage tank 14 is then fed into the tube 18, of which the valve 22 is opened, using the injection pump 12, and atmospheric air is fed in conjunction with the reducing agent into the tube 18, of which the valve 22 is opened, using the air pump 16.
Additionally, air and the reducing agent fed into the tube 18, of which the valve 22 is opened, are sprayed into the exhaust gas containing nitrogen oxides flowing in the reactor 4 through the nozzles 8 of the tube 18.
Further, the exhaust gas mixed with the reducing agent passes through the catalytic beds 10 positioned behind the nozzles 8 to reduce nitrogen oxides contained in the exhaust gas into nitrogen.
Subsequently, the treated exhaust gas is discharged through the outlet pipe 6 connected to the ending part of the reactor 4. Compressed air from the air pump 16 is fed in conjunction with the reducing agent into the nozzles 8, which allows that the exhaust gas is readily mixed with the reducing agent.
A better understanding of the present invention may be obtained through the following examples which are set forth to illustrate, but not to be construed as to limit of the present invention.
Production of Non-Sulfuric Acid-Treated Catalytic Bed 1
Alumina [Spheralite 557, Exxons, France] was slowly added to ion-exchanged water with strong agitation to produce a homogeneous slurry.
The slurry was coated on a cordierite honeycomb body [Facktop Kocat, China] with a size of 15×15×10 cm and cell density of 200 cells/in2 (84×84 cells) so that a ratio of alumina to the cordierite honeycomb body was 0.111 g/cm3, and then dried at room temperature for 24 hours.
The dried honeycomb body was again dried at 120° C. for 4 hours and then heated at a rate of 10° C./min to 600° C., and calcined at 600° C. for 2 hours.
The calcined honeycomb body on which alumina was coated was placed in a silver nitrate aqueous solution (AgNO3)[Hangyeol Gold, Korea] so that the silver content in the resulting honeycomb body was 2.1 wt % based on alumina, and then dried at room temperature for 24 hours.
The resulting honeycomb body was then dried at 120° C. for 4 hours, heated at a rate of 10° C./min to 600° C. and then calcined at 600° C. for 2 hours.
Production of Non-Sulfuric Acid-Treated Catalytic Bed 2
The procedure of example 1 was repeated with the exception that the ratio of alumina to the cordierite honeycomb body, was 0.123 g/cm3 instead of 0.111 g/cm3, and the silver content in the resulting honeycomb body was 5.0 wt % instead of 2.1 wt % based on alumina.
Production of Non-Sulfuric Acid-Treated Catalytic Bed 3
The procedure of example 1 was repeated except that the ratio of alumina to the cordierite honeycomb body was 0.149 g/cm3 instead of 0.111 g/cm3, and the silver content in the resulting honeycomb body was 6.0 wt % instead of 2.1 wt % based on alumina.
Production of Sulfuric Acid-Treated Catalytic Bed 1
The catalytic bed produced according to example 2 was placed in 0.1 M sulfuric acid aqueous solution [sulfuric acid, Duk-san Pharmaceutical Industry Co. Ltd., Korea], and dried at room temperature for 24 hours.
The dried catalytic bed was again dried at 120° C. for 4 hours, heated at a rate of 10° C./min to 500° C., and calcined at 500° C. for 2 hours to produce the sulfuric acid-treated catalytic bed.
The produced sulfuric acid-treated catalytic bed had a ratio of alumina to the honeycomb body of 0.123 g/cm3, a silver content in the resulting catalytic bed of 5.0 wt % based on alumina, and a sulfate (SO42−) content in the resulting catalytic bed of 1 wt % based on alumina.
Production of Sulfuric Acid-Treated Catalytic bed 2
The procedure of example 4 was repeated except that 0.21 M sulfuric acid aqueous solution was used instead of 0.1 M sulfuric acid aqueous solution.
The produced sulfuric acid-treated catalytic bed had a ratio of alumina to the honeycomb body of 0.123 g/cm3, a silver content in the resulting catalytic bed of 5.0 wt % based on alumina, and a sulfate (SO42−) content in the resulting catalytic bed of 2 wt % based on alumina.
Production of Sulfuric Acid-treated Catalytic Bed 3
The procedure of example 4 was repeated except that 0.42 M sulfuric acid aqueous solution was used instead of 0.1 M sulfuric acid aqueous solution.
The resulting sulfuric acid-treated catalytic bed had a ratio of alumina to the honeycomb body of 0.123 g/cm3, a silver content in the resulting catalytic bed of 5.0 wt % based on alumina, and a sulfate (SO42−) content in the resulting catalytic bed of 4 wt % based on alumina.
As shown in
The catalytic bed according to example 1 was installed behind the tube having a plurality of nozzles in the reactor.
Ethanol [Duk-san Pharmaceutical Industry Co. Ltd., Korea] acting as a reducing agent was charged into a storage tank. The storage tank was connected to an injection pump [M930, Younglin Co., Korea] that was connected to the tube with the nozzles.
An air pump [HP 2.5, Air bank compressor Co., Korea] was then connected to the tube with the nozzles to feed compressed air into the reactor.
Exhaust gas discharged from a LPG (liquefied petroleum gas) burner [Eg02.9R, Elco, Germany] of a boiler [Jewoo royal steam boiler, Jewoo energy, Korea] and nitrogen monoxide [Metson, USA] were fed into the reactor, and the flow rate of the exhaust gas and nitrogen monoxide was controlled by using a mass flow controller [F-201C-FAC-22-V, Bronchost, Netherlands].
The flow rate and the composition of the exhaust gas are described in Table 1.
When the exhaust gas that was fed into the reactor passed through the inlet pipe, high pressure air and ethanol were simultaneously fed into the nozzles using both the air pump and injection pump so as to be sprayed into the exhaust gas passing through the reactor.
The molar ratio of ethanol to nitrogen oxides fed into the reactor was controlled to be 1, and a K-type thermocouple was installed in the reactor to measure the temperature in the reactor.
Reaction conditions were controlled in such a way that the temperature in the reactor was 100 to 550° C. and the space velocity was 20,000 h−1. The space velocity was calculated using the following equation 1.
The concentration of the exhaust gas was analyzed by a portable nitrogen oxides analyzer[MK 2, Eurotron, Italy] before and after the reaction of nitrogen oxides with ethanol. Conversion efficiency of nitrogen oxide was calculated using the following Equation 2. The calculated results are shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 2 was used instead of using the catalytic bed according to example 1.
The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 5 was used instead of using the catalytic bed according to example 1.
The results are shown in
As shown in
The procedure of example 7 was repeated except that a gasoline burner [OM-1, Olympia Co., Korea] was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The temperature in the reactor ranged from 200 to 550° C. The space velocity was 20,000 h−1.
The flow rate and the composition of the exhaust gas are described in Table 2.
The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 2 was used instead of the catalytic bed according to example 1. A gasoline burner was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The temperature in the reactor ranged from 200 to 550° C. The space velocity was 20,000 h−1.
The composition of the exhaust gas fed into the reactor is described in Table 2. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated that except the catalytic bed according to example 3 was used instead of the catalytic bed according to example 1. A gasoline burner was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The temperature in the reactor ranged from 200 to 550° C. The space velocity was 20,000 h−1.
The composition of the exhaust gas fed into the reactor is described in Table 2. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that an internal combustion power plant [5.6MW, 14PC 2.5V DF, Nikata, Japan] using 90% LNG+10% gasoline as a fuel was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The reactor temperature was 450° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The flow rate and the composition of the exhaust gas fed into the reactor are described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated with the exception that the catalytic bed according to example 4 was used instead of the catalytic bed according to example 1. The internal combustion power plant using 90% LNG+10% gasoline as a fuel was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The reactor temperature was 450° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 5 was used instead of the catalytic bed according to example 1. An internal combustion power plant using 90% LNG+10% gasoline as a fuel was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The reactor temperature was 450° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 6 was used instead of the catalytic bed according to example 1. An internal combustion power plant using 90% LNG+10% gasoline as a fuel was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The reactor temperature was 450° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
As shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 2 was used instead of the catalytic bed according to example 1. An internal combustion power plant using 90% LNG+10% gasoline as a fuel was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The reactor temperature ranged from 200 to 550° C. At this time, the flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
The procedure of example 7 was repeated except that the catalytic bed according to example 4 was used instead of the catalytic bed according to example 1. In an early stage, 100% gasoline was used as a fuel, and in a stable stage, an internal combustion power plant using 90% LNG+10% gasoline was used instead of the LPG burner in example 7. The molar ratio of ethanol to nitrogen oxides was 2. The temperature in the reactor temperature ranged from 200 to 550° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
As can be seen in
The procedure of example 7 was repeated except that the catalytic bed according to example 2 was used instead of the catalytic bed according to example 1. The exhaust gas discharged from an internal combustion power plant using 90% LNG+10% gasoline as a fuel instead of the LPG burner was used as a subjecting gas. The molar ratio of ethanol to nitrogen oxides was 1. The temperature in the reactor ranged from 200 to 550° C. The flow rate of the exhaust gas was controlled in such a way that the space velocity was 20,000 h−1 at a hybrid mode (90% LNG+10% gasoline) in which the composition and concentration of the exhaust gas were stable after the internal combustion power plant was operated.
The composition of the exhaust gas fed into the reactor is described in Table 3. The calculated conversion efficiency of nitrogen oxide for this system is shown in
As can be seen in
As shown in
The catalytic bed produced according to example 2 was installed at the rear of the tube including a plurality of nozzles, and then another set of catalytic bed and tube as above was installed in the rear part of the reactor.
Ethanol, acting as the reducing agent, was injected into a storage tank that was connected to an injection pump. The injection pump was connected to the tube with the nozzles.
An air pump was then connected to the tube with the nozzles and fed high pressure air into the reactor.
Exhaust gas discharged from an internal combustion power plant using 90% LNG+10% gasoline as the fuel and a separate nitrogen monoxide were fed into the front part of the reactor. The flow rates of the exhaust gas and nitrogen monoxide were controlled using a mass flow controller.
Compositions and concentrations of gases fed into the reactor were described in Table 3. Reaction conditions were controlled in such a way that the temperature in the reactor ranged from 200 to 500° C., and the space velocity was 20,000 h−1.
At this time, the molar ratio of ethanol sprayed into the exhaust gas through each of the tubes, including a plurality of nozzles, to nitrogen oxides was 0.5. The procedure of analyzing the resulting product was conducted as the same procedure as example 7.
The results are shown in
The procedure of example 20 was repeated except that the molar ratio of ethanol to nitrogen oxides for each tube was 1 instead of 0.5. The procedure of analyzing the resulting product was conducted as the same procedure as example 7. The results are shown in
The procedure of example 20 was repeated except that 100% gasoline was used as a fuel of an internal combustion power plant instead of using a mixture of 90% LNG+10% gasoline. A flow rate and composition of exhaust gas fed into a reactor are described in Table 4. The procedure of analyzing the resulting product was conducted as the same procedure as example 7. The results are shown in
From
As shown in
The catalytic bed was installed according to example 1 behind the tube having a plurality of nozzles in the reactor.
Ethanol [Duk-san Pharmaceutical Industry Co. Ltd., Korea] acting as a reducing agent was charged into a storage tank. The storage tank was connected to an injection pump [M930, Younglin Co., Korea] that was connected to the tube with the nozzles.
An air pump [HP 2.5, Air bank compressor Co., Korea] was then connected to the tube with the nozzles to feed compressed air into the reactor.
The exhaust gas discharged from a LPG (liquefied petroleum gas) burner [Eg02.9R, Elco, Germany] of a boiler [Jewoo royal steam boiler, Jewoo energy, Korea] and nitrogen monoxide [Metson, USA] were fed into the reactor. The flow rates of the exhaust gas and nitrogen monoxide were controlled by using a mass flow controller [F-201C-FAC-22-V, Bronchost, Netherlands].
The flow rate and a composition of the exhaust gas are described in Table 5, below.
When the exhaust gas that was fed into the reactor passed through the inlet pipe, high pressure air and ethanol were simultaneously fed into the nozzles using both the air pump and injection pump so as to be sprayed into the exhaust gas passing through the reactor.
The molar ratio of ethanol to nitrogen oxides fed into the reactor was controlled to be 2. Reaction conditions were controlled in such a way that the temperature in the reactor was 200 to 550° C., and the space velocity was 20,000 h−1.
The generation rate of N2O was calculated according to Equation 3. The calculated results are shown in
The procedure of example 23 was repeated except that the catalytic bed according to example 4 was used instead of using the catalytic bed according to example 1. The generation rate of N2O was calculated according to Equation 3. The calculated results are shown in
The procedure of example 23 was repeated except that the catalytic bed according to example 5 was used instead of using the catalytic bed according to example 1. The generation rate of N2O was calculated according to Equation 3. The calculated results are shown in
The procedure of example 23 was repeated except that the catalytic bed according to example 6 was used instead of using the catalytic bed according to example 1. The generation rate of N2O was calculated according to Equation 3. The calculated results are shown in
As can be seen in
As described above, the present invention is advantageous in that the procedure of producing a catalytic bed can be varied, depending on the conditions of the exhaust gas from a stationary and a mobile source using gases or liquid oils as a fuel, such as gasoline, kerosene or bio-diesel oil. The present invention can effectively reduce nitrogen oxides to nitrogen and water by spraying a reducing agent into the exhaust gas according to a multi-injection manner in the presence of the catalytic bed.
The present invention is also advantageous in that the present invention utilizing ethanol as the reducing agent can improve the relatively low conversion efficiency of nitrogen oxides of a conventional HC-SCR process.
While this invention has been particularly shown and described with references to preferred embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the invention encompassed by the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10-2003-0028926 | May 2003 | KR | national |
| 10-2004-0020956 | Mar 2004 | KR | national |
