Metal tungstates for use as nitrogen oxides reduction catalysts

Abstract

A nitrogen oxide (NOx) reduction catalyst that includes a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu. The catalyst may be utilized in various environments including oxygen rich and oxygen deficient environments.

Claims

1. A process of reducing nitrogen oxide (NOx) including the steps of: providing a gaseous exhaust mixture including nitrogen oxide (NOx) and hydrocarbon fuel; providing a nitrogen oxide (NOx) reduction catalyst including a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu; contacting the gaseous exhaust mixture with a surface of the nitrogen oxide (NOx) reduction catalyst forming nitrogen, water and carbon dioxide.

2. The process of claim 1 wherein the gaseous exhaust mixture further includes oxygen.

3. The process of claim 2 wherein the nitrogen oxide (NOx) reduction catalyst includes a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co and Cu.

4. The process of claim 1 wherein the nitrogen oxide (NOx) reduction catalyst includes a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Ni and Co and the catalyst reduces nitrogen oxide (NOx) in an oxygen deficient environment.

5. The process of claim 1 wherein the transition metal tungstate includes a crystalline structure.

6. The process of claim 1 wherein the transition metal tungstate has a particle size of from 10 to 60 nanometers.

7. The process of claim 1 wherein the catalyst has the formula: MnWO.sub.4 and the catalyst reduces nitrogen oxide (NOx) in the presence of oxygen.

8. The process of claim 7 wherein the catalyst has significant selectivity to NOx conversion in the presence of oxygen such that the nitrogen oxide (NOx) conversion and oxygen conversion are approximately equal to one another.

9. The process of claim 7 wherein the catalyst has nitrogen oxide (NOx) conversion that is greater than 90 percent.

10. A process of reducing nitrogen oxide (NOx) including the steps of: providing a gaseous exhaust mixture including nitrogen oxide (NOx) and hydrocarbon fuel; providing a nitrogen oxide (NOx) reduction catalyst including a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co and Cu; contacting the gaseous exhaust mixture with a surface of the nitrogen oxide (NOx) reduction catalyst in the presence of oxygen and forming nitrogen, water and carbon dioxide.

11. A process of reducing nitrogen oxide (NOx) including the steps of: providing a gaseous exhaust mixture including nitrogen oxide (NOx) and hydrocarbon fuel; providing a nitrogen oxide (NOx) reduction catalyst including a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu; contacting the gaseous exhaust mixture with a surface of the nitrogen oxide (NOx) reduction catalyst in an oxygen deficient environment and forming nitrogen, water and carbon dioxide.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1A is a scanning electron microscopy (SEM) image of MnWO.sub.4 nanoparticles;

(2) FIG. 1B is a scanning electron microscopy (SEM) image of CoWO.sub.4 nanoparticles;

(3) FIG. 1C is a scanning electron microscopy (SEM) image of FeWO.sub.4 nanoparticles;

(4) FIG. 1D is a scanning electron microscopy (SEM) image of NiWO.sub.4 nanoparticles;

(5) FIG. 1E is a scanning electron microscopy (SEM) image of CuWO.sub.4 nanoparticles;

(6) FIG. 2 is a plot of the particle size and corresponding specific surface area (BET SSA) for MWO.sub.4 wherein M is selected from Mn, Fe, Co, Ni, and Cu;

(7) FIG. 3 is a graphical depiction of the testing protocol used for activity tests of the nitrogen oxide (NOx) reduction catalyst;

(8) FIG. 4 is a plot of the NO conversion as a function of temperature for the nitrogen oxide (NOx) reduction catalyst without oxygen;

(9) FIG. 5 is a plot of the NO conversion as a function of temperature for the nitrogen oxide (NOx) reduction catalyst with oxygen;

(10) FIG. 6 is a plot of the NO conversion as a function of oxygen conversion for the nitrogen oxide (NOx) reduction catalyst;

(11) FIG. 7 is a plot of the NO, oxygen and hydrocarbon conversion as a function of the temperature for MnWO.sub.4;

(12) FIG. 8 is a plot of the nitrogen and nitrogen dioxide counts as a function of temperature for MnWO.sub.4;

(13) FIG. 9 is a plot of the NO and hydrocarbon conversion as a function of the temperature for NiWO.sub.4;

(14) FIG. 10 is a plot of the nitrogen and nitrogen dioxide counts as a function of temperature for NiWO.sub.4;

(15) FIG. 11 is an XRD plot of MWO.sub.4 wherein M is selected from Mn, Fe, Co, Ni, and Cu;

(16) FIG. 12 is a graphical representation of a reduction mechanism for the nitrogen oxide (NOx) reduction catalyst in an oxygen rich condition;

(17) FIG. 13 is a graphical representation of a reduction mechanism for the nitrogen oxide (NOx) reduction catalyst in an oxygen deficient condition.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

(18) The present disclosure provides a method of forming, process of reducing nitrogen oxide (NOx) and/or catalyst composition for the reduction of nitrogen oxide (NOx) to generate nitrogen, water and carbon dioxide. The catalyst may include a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu. The catalyst may be utilized in oxygen rich environments and oxygen deficient environments. This catalyst provides a precious metal free catalyst that allows for reaction in a variety of conditions unlike most 3-way catalysts that operate only in narrowly defined conditions. The catalyst allows the selective interaction of nitrogen oxide (NOx) with a surface of the catalyst in oxygen rich and oxygen deficient environments in contrast to current prior art catalysts.

(19) The process includes providing a gaseous exhaust mixture including nitrogen oxide (NOx) and hydrocarbon fuel; providing a nitrogen oxide (NOx) reduction catalyst including a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu; and contacting the gaseous exhaust mixture with a surface of the nitrogen oxide (NOx) reduction catalyst forming nitrogen, water and carbon dioxide.

(20) In one aspect the nitrogen oxide (NOx) reduction catalyst includes the transition metal tungstate of the formula MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu and includes a crystalline structure. The catalyst can include a plurality of transition metal tungstate nanoparticles. In some instances, the nanoparticles are uniform in size and can have an average particle size of 10 to 60 nanometers as best shown in FIGS. 1A-E and FIG. 2.

(21) As described above, the catalyst may be used in a variety of conditions such as oxygen rich and oxygen deficient conditions. In one aspect, the catalyst may have the formula: MWO.sub.4 wherein M is selected from Mn, Fe, Co and Cu and the catalyst reduces nitrogen oxide (NOx) in an oxygen rich environment.

(22) In another aspect, the catalyst may have the formula: MWO.sub.4 wherein M is selected from Ni and Co and the catalyst reduces nitrogen oxide (NOx) in an oxygen deficient environment.

(23) In another aspect, there is disclosed a process of forming a nitrogen oxide (NOx) reduction catalyst including the steps of: providing metal salts of the transition metal including Co(NO.sub.3).sub.2, MnCl.sub.2, Fecl.sub.2, Ni(NO.sub.3).sub.2 or Cu(SO.sub.4).sub.4; providing Na.sub.2WO.sub.4; combining the metal salt and Na.sub.2WO.sub.4 forming a solution; exposing the solution to a source of microwave energy and initiating a hydrothermal reaction forming MWO.sub.4. The exposing step may include exposure to microwave energy for various periods of time to elevate the temperature or heat the solution to a desired temperature range.

(24) The exposing step may include exposing the solution to microwave energy from less than one minute to 60 minutes. In one aspect, the exposing step may be from 1 to 10 minutes at a power of 800 Watts. The exposing step may raise the temperature of the solution to a temperature of from 80 to 300 degrees C. Following the exposing step, the solution may be cooled and then washed and dried. Following the drying step, the catalyst material may be calcined in air at 350-700 degrees C. for 60 minutes.

(25) For an oxygen rich condition the catalyst may include a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Mn, Fe, Co and Cu wherein the catalyst reduces nitrogen oxide (NOx) with hydrocarbon fuel.

(26) Referring to FIG. 12, there is shown a graphical depiction of the catalyst reaction in an oxygen rich condition. As shown in the figure, oxygen adsorbs to a surface of the catalyst and nitrogen oxide (NOx) in the form of nitric oxide (NO, x=1) bonds with the surface adsorbed oxygen forming nitrogen dioxide which reacts with the hydrocarbon fuel forming nitrogen, carbon dioxide and water. The reaction mechanism as described may reduce the overall activation energy barrier for (NOx) or (NO) reduction in typical prior art catalysts.

(27) For the oxygen deficient condition the catalyst may include a transition metal tungstate having the formula: MWO.sub.4 wherein M is selected from the group consisting of Ni and Co wherein the catalyst reduces nitrogen oxide (NOx) an oxygen deficient environment including hydrocarbon fuel.

(28) Referring to FIG. 13, there is shown a graphical depiction of the catalyst reaction in an oxygen deficient condition. As shown in the figure, nitrogen oxide (NOx) or (NO) bonds with a surface of the catalyst and the nitrogen oxygen bonds dissociate forming nitrogen and the oxygen reacts with the hydrocarbon fuel forming carbon dioxide and water.

(29) The invention is further described by the following examples, which are illustrative of specific modes of practicing the invention and are not intended as limiting the scope of the invention defined in the claims.

EXAMPLES

(30) Preparation of MWO.sub.4.

(31) Starting materials of Co(NO.sub.3).sub.2, MnCl.sub.2, Fecl.sub.2, Ni(NO.sub.3).sub.2 or Cu(SO.sub.4).sub.4 and Na.sub.2WO.sub.4.2H.sub.2O were purchased from Sigma-Aldrich and used directly without further purification. In a typical synthesis a (0.2M) Na.sub.2WO.sub.4 solution was combined with a (0.2M) transition metal solution in a stoichiometric manner with strong agitation. The solution mixture was then placed into a glass microwave tube. A microwave assisted hydrothermal synthesis was conducted on a microwave reactor (Anton Paar Microwave 300). The microwave tube was heated to various temperatures at max power (800 W). The exposure to microwaves was maintained for various times as will be discussed in more detail below. Following the exposure to microwaves the tube was cooled by forced air flow. The resulting product was rinsed with DI water multiple times on a centrifuge followed by vacuum drying overnight at 60 degrees C. Following the drying step, the catalyst material was calcined in air at 550 degrees C. for 60 minutes.

(32) A final powder product was examined by scanning electron microscopy (SEM) as shown in FIGS. 1A-E. It can be seen in the Figures that MWO.sub.4 material includes discrete particles having a size ranging from 10-60 nm. The particles have a specific surface area of from 4.9 to 28.2 m.sup.2/g as depicted in FIG. 2. X-ray diffraction (XRD) data is shown in FIG. 11 and shows a crystalline structure for the catalyst materials.

Example II

(33) Activity Testing MWO.sub.4

(34) The activity testing was performed in a laboratory scale packed bed reactor (PID Eng&Tech Microactivity-Reference). Activity was determined for NO reduction by the hydrocarbon propylene (C3H6). Activity testing was performed under stoichiometric conditions both in oxygen deficient and oxygen rich conditions. As depicted in FIG. 3, under oxygen deficient conditions, the stoichiometric ratio of NO:C3H6 is 9:1, and under oxygen rich conditions, the stoichiometric ratio of NO:C3H6:O2 is 3:1:3. Also depicted in FIG. 3, 100 mg of catalyst material was combined with 400 mg of quartz sand and a total flowrate of 100 ml/min (gas hour space velocity GHSV 15,000 inverse hours) was used for the testing in both oxygen rich and oxygen deficient conditions. A pretreatment phase includes heating the reactor and catalyst mixture to 500 degrees C. and maintaining the temperature for 15 minutes under oxidizing conditions (30 ml/min of 10% O2 in He balance). The reactor is then cooled and maintained at 50 degrees C. for a specified time with the introduction of the gaseous mixture of nitrogen oxide (NOx) in the form of nitric oxide (NO, x=1), hydrocarbon (C.sub.3H.sub.6) and oxygen in certain tests. The reactor is then heated to 600 degrees C. Measurements were taken at various temperatures as reflected in the various data which will be discussed in more detail below.

(35) Referring to FIG. 4, there is shown a plot of the NO conversion over the catalyst samples in an oxygen deficient condition in which no oxygen was added to the reactor. As can be seen from the plot, the NiWO.sub.4 and CoWO.sub.4 samples exhibited NO reduction in the oxygen deficient condition. The reduction of NOx in the oxygen deficient condition verifies the selective interaction of NO with the catalyst surface in the absence of oxygen.

(36) Referring to FIG. 5 there is shown a plot of the NO conversion over the catalyst samples in an oxygen rich condition in which oxygen was added to the reactor. As can be seen from the plot, the MnWO.sub.4, FeWO.sub.4, CoWO.sub.4 and CuWO.sub.4 samples exhibited NO reduction in the oxygen rich condition. The reduction of NOx in the oxygen rich condition verifies the selective interaction of NO with the catalyst surface in the presence of oxygen.

(37) FIG. 6 depicts a plot of the NO conversion over the catalyst samples as a function of the O.sub.2 conversion under the conditions of stoichiometric NO reduction under oxygen rich conditions in which oxygen was added to the reactor. As can be seen from the plot, the MnWO.sub.4, FeWO.sub.4, CoWO.sub.4 samples exhibit significant NO selectivity. The selectivity herein refers to the ability of the catalyst surface to selectively interact with NO gas rather than O.sub.2 gas. The MnWO.sub.4 sample displays an almost 1 to 1 selectivity of NO to O.sub.2. The ability of the catalyst surface to perform the desired NO reduction reaction in the presence of oxygen provides an improvement over current prior art catalysts.

(38) Referring to FIG. 7, there are shown NO, C3H6, and O2 conversions as a function of temperature for MnWO.sub.4 in an oxygen rich condition in which oxygen was added to the reactor. As can be seen in the figure, the NO conversation exceeds 90% for the sample. The NO conversion dropped as O.sub.2 was depleted at higher temperatures.

(39) Referring to FIG. 8, production of N2 and NO2 as monitored by the detection of the mass spectrometry counts at m/z=28 and m/z=46, respectively, are shown as a function of temperature in an oxygen rich condition in which oxygen was added to the reactor. FIG. 8 indicates that reduction of NO under oxygen rich conditions results in the production of N.sub.2 with trace amounts of NO.sub.2 also present.

(40) Referring to FIG. 9, there are shown NO and C3H6 conversions as a function of temperature for NiWO.sub.4 in an oxygen deficient condition in which no oxygen was added to the reactor. As can be seen in the figure, the NO conversation exceeds 80% for the sample.

(41) Referring to FIG. 10, production of N2 and NO2 as monitored by the detection of the mass spectrometry counts at m/z=28 and m/z=46, respectively, are shown as a function of temperature in an oxygen deficient condition in which no oxygen was added to the reactor. FIG. 10 indicates that reduction of NO under oxygen deficient conditions results in the production of N.sub.2 and with no production of NO.sub.2.

(42) The invention is not restricted to the illustrative examples described above. Examples described are not intended to limit the scope of the invention. Changes therein, other combinations of elements, and other uses will occur to those skilled in the art. The scope of the invention is defined by the scope of the claims.