Mn/CeO2 catalyst for dimethyl ether production via oxidative dehydration of methanol

Abstract

A method of producing dimethyl ether involving contacting methanol with a catalyst in the presence of oxygen in a reactor to form the dimethyl ether. The catalyst comprises manganese on a cerium oxide catalyst support, wherein a weight ratio of manganese to the cerium oxide catalyst support is in the range of 0.005 to 0.5. Further, a method of manufacturing the catalyst, including mixing cerium oxide (CeO.sub.2) with a solution comprising manganese salt and a solvent, evaporating the solvent, followed by drying and calcining to form a catalyst which comprises manganese on a cerium oxide catalyst support, wherein a weight ratio of manganese to the cerium oxide catalyst support is in the range of 0.005 to 0.5.

Claims

1. A method of producing dimethyl ether comprising: contacting a mixture of methanol and oxygen with a catalyst in a reactor to form the dimethyl ether via oxidative dehydration of methanol, wherein the catalyst consists of manganese on a cerium oxide catalyst support, wherein a weight ratio of manganese to the cerium oxide catalyst support is in the range of 0.005 to 0.5.

2. The method of claim 1, wherein the reactor is a fixed bed reactor.

3. The method of claim 1, wherein 1 to 20 mol % of the methanol is converted to dimethyl ether.

4. The method of claim 1, wherein methanol and oxygen are contacted with the catalyst at a temperature in the range of 275 C. to 450 C.

5. The method of claim 1, wherein a selectivity of dimethyl ether from a conversion of 50 to 100 mol % methanol is in the range of 20 to 100%.

6. The method of claim 1, wherein a molar ratio of oxygen to methanol in the mixture of methanol and oxygen is in the range of 0.1:1 to 1:1.

7. The method of claim 1, wherein 20 to 100 mol % of the oxygen is converted to dimethyl ether.

8. The method of claim 1, wherein the catalyst consists of the manganese on a solid porous cerium oxide catalyst support.

9. The method of claim 1, wherein the catalyst does not comprise a zeolite.

10. The method of claim 1, wherein 1 to 50 mol % of the methanol is converted to dimethyl ether.

11. The method of claim 1, wherein the catalyst consists of the manganese as the only active metal on a solid porous cerium oxide catalyst support.

12. The method of claim 1, wherein the catalyst is prepared by mixing cerium oxide with a solution comprising manganese salt and a solvent; evaporating the solvent to form a solid; drying and calcining the solid at a temperature in the range of 100 to 500 C. to form the catalyst, which consists of manganese on a cerium oxide catalyst support, wherein a weight ratio of manganese to the cerium oxide catalyst support is in the range of 0.005 to 0.5.

13. The method of claim 12, further comprising: granulating the catalyst to form catalyst grains with a grain size in the range of 0.05 mm to 0.5 mm.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) A more complete appreciation of the disclosure and many of the attendant advantages thereof will be readily obtained as the same becomes better understood by reference to the following detailed description when considered in connection with the accompanying drawings, wherein:

(2) FIG. 1 shows XRD patterns of a CeO.sub.2 catalyst, a 1% Mn/CeO.sub.2 catalyst, a 3% Mn/CeO.sub.2 catalyst, and a 5% Mn/CeO.sub.2 catalyst.

(3) FIG. 2 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 1% Mn/CeO.sub.2 catalyst, in the absence of an O.sub.2 flow.

(4) FIG. 3 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 1% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0.2.

(5) FIG. 4 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 1% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0.2.

(6) FIG. 5 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 1% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0.5.

(7) FIG. 6 is a graph depicting a DME yield vs. temperature in the presence of the 1% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0, 0.2, 0.3, and 0.5.

(8) FIG. 7 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 3% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0.5.

(9) FIG. 8 is a graph depicting a methanol conversion and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the 5% Mn/CeO.sub.2 catalyst, wherein a molar ratio of O.sub.2 to methanol is 0.5.

(10) FIG. 9 is a graph depicting a DME yield vs. temperature in the presence of the 1% Mn/CeO.sub.2, the 3% Mn/CeO.sub.2, and the 5% Mn/CeO.sub.2 catalysts.

(11) FIG. 10 is a graph depicting data of a stability test of the 1% Mn/CeO.sub.2 catalyst.

(12) FIG. 11 is a graph depicting data of a stability test of the 3% Mn/CeO.sub.2 catalyst.

(13) FIG. 12 is a graph depicting methanol and oxygen conversions and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of the cerium oxide catalyst;

(14) FIG. 13 is a graph depicting a DME yield vs. temperature in the presence of the cerium oxide catalyst and the 1% Mn/CeO.sub.2 catalyst.

(15) FIG. 14 is a graph depicting methanol and oxygen conversions and selectivity percentiles with respect to hydrogen, carbon monoxide, carbon dioxide, formaldehyde, and dimethyl ether, for reactions in the presence of a manganese oxide catalyst (i.e. MnOx).

(16) FIG. 15 is a graph depicting a DME yield vs. temperature in the presence of the manganese oxide catalyst and the 1% Mn/CeO.sub.2 catalyst.

DETAILED DESCRIPTION OF THE EMBODIMENTS

(17) According to a first aspect, the present disclosure relates to a method for producing dimethyl ether involving contacting methanol with a catalyst in a reactor to form the dimethyl ether (DME). The catalyst comprises manganese on a cerium oxide catalyst support. In some embodiments, the catalyst may include manganese oxide, manganese, or both and cerium oxide.

(18) Referring now to FIG. 1, in some embodiments, the catalyst includes manganese and the cerium oxide catalyst support, wherein a weight ratio of manganese to the catalyst support is in the range of 0.005 to 0.5, preferably 0.01 to 0.3, preferably 0.01 to 0.1, preferably 0.01 to 0.05, preferably 0.02 to 0.05. FIG. 1 depicts an X-Ray diffraction pattern for an exemplary CeO.sub.2 catalyst (FIG. 1102), an exemplary 1 wt % Mn/CeO.sub.2 catalyst (FIG. 1104), an exemplary 3 wt % Mn/CeO.sub.2 catalyst (FIG. 1106), and an exemplary 5 wt % Mn/CeO.sub.2 catalyst (FIG. 1108).

(19) The catalyst of manganese on a cerium oxide catalyst support may also be denoted as Mn/CeO.sub.2 in this disclosure.

(20) The term catalyst support refers to a solid substrate, wherein manganese particles are deposited. The catalyst support may preferably a porous solid that provides a higher surface area for contacting methanol, preferably in the presence of oxygen. Accordingly, in a preferred embodiment, the Mn/CeO.sub.2 catalyst has a Brunauer-Emmett-Teller (BET) surface area in the range of 5 m.sup.2/g to 15 m.sup.2/g, preferably 6 m.sup.2/g to 14 m.sup.2/g, preferably 7 m.sup.2/g to 13 m.sup.2/g, preferably 7 m.sup.2/g to 12 m.sup.2/g.

(21) The grain size of the Mn/CeO.sub.2 catalyst might affect the rate and the selectivity of the oxidative dehydration reactions of methanol, due to the diffusion limitations of methanol or reaction products. Therefore, in some embodiments, the Mn/CeO.sub.2 catalyst are granulated and sieved to form catalyst grains with a grain size in the range of 0.05 mm to 0.5 mm, preferably 0.75 mm to 0.4 mm, preferably 0.1 mm to 0.3 mm, preferably 0.2 mm to 0.25 mm.

(22) In the oxidative dehydration of methanol to DME, side products may also be formed. In some embodiments, the side product may be hydrogen, carbon monoxide, carbon dioxide, formaldehyde, or a combination thereof. The formation of the side products is not an objective of the present disclosed catalyst or the method.

(23) In a preferred embodiment, a selectivity of dimethyl ether from a conversion of 50 to 100 mol %, preferably 60 to 95 mol %, preferably 70 to 90 mol % methanol is in the range of 20 to 100%, preferably 30 to 95%, preferably 40 to 90%, preferably 50 to 85%, preferably 60 to 85%, preferably 65 to 80%. The term selectivity as used herein refers to a percentile of dimethyl ether produced in moles per moles of methanol consumed. Furthermore, the term conversion of methanol refers to a ratio (in percentile) of moles of methanol that is converted in a reactor (i.e. an amount (in mole) of methanol that enters a reactor subtracted by an amount (in mole) of methanol that exits the reactor), relative to the moles of methanol that enters the reactor. The calculations are further described in the Examples herein.

(24) FIG. 2 represents a diagram of exemplary data of methanol contacting the Mn/CeO.sub.2 catalyst in the absence of an oxygen flow. The results depict a low conversion less than or equal to 20 mol %, preferably less than or equal to 10 mol %. A slight increase in the methanol conversion rate at elevated temperatures (i.e. above 350 C., preferably above 400 C.) is observed.

(25) An implementation of the presently disclosed method increases the conversion of methanol to dimethyl ether by contacting the catalyst with a mixture of methanol and oxygen. The mixture of methanol and oxygen has a molar ratio of oxygen to methanol in the range of 0.1:1 to 1:1, preferably 0.1:1 to 0.6:1, preferably 0.2:1 to 0.6:1, preferably 0.2:1 to 0.5:1. FIG. 3, FIG. 4, and FIG. 5 depict data from three exemplary catalyst reaction tests of the catalyst having a 1% Mn/CeO.sub.2, wherein a molar ratio of oxygen to methanol is 0.2:1, 0.3:1, and 0.5:1, respectively. In some embodiments, as shown in FIGS. 3, 4 and 5, 10 mol % to 50 mol %, preferably 10 mol % to 40 mol %, preferably 10 mol % to 30 mol % of the methanol is converted to dimethyl ether or at least one side product (hydrogen, carbon monoxide, carbon dioxide, and formaldehyde). Selectivity of dimethyl ether from the conversion of methanol may depend on the reaction temperature. Therefore, in all embodiments, a temperature of the reactor is in the range of 275 C. to 450 C., preferably 275 C. to 400 C., preferably 275 C. to 350 C. Accordingly, the selectivity of dimethyl ether is in the range of 75 mol %-85 mol % or 80 mol % to 90 mol % in the temperature range between in the range of 275 C. to 450 C., preferably 275 C. to 400 C., preferably 275 C. to 350 C. in the presence of an O.sub.2 flow. The side products formed may be in the range of 0 to 20%, preferably 0 to 15%, more preferably 0 to 10% of the converted methanol in the above reaction temperature ranges.

(26) In one embodiment, 20 mol % to 100 mol %, preferably 30 mol % to 100 mol %, more preferably 40 mol % to 100 mol % of the oxygen is converted to dimethyl ether or at least one of carbon monoxide, carbon dioxide, formaldehyde, and/or water.

(27) In one embodiment, the catalyst remains stable during oxidative dehydration reactions in the reaction temperature of 275 C. to 450 C., preferably 275 C. to 400 C., preferably 275 C. to 375 C., preferably 300 C. to 375 C., for at least 50 hours, preferably at least 60 hours, preferably at least 65 hours, preferably at least 70 hours, preferably at least 75 hours, preferably at least 80 hours, preferably at least 85 hours, preferably at least 90 hours, preferably at least 95 hours, preferably at least 100 hours. The catalyst's stability may be measured by a percent of deactivation. The term deactivation as used herein refers to a loss of catalytic activity (as a measure of reaction rate decrease with time), which classifies as deactivation by type (chemical, thermal, and mechanical) and by mechanism (poisoning, fouling, thermal degradation, vapor formation, vapor-solid and solid-solid reactions, and attrition/crushing). In one embodiment, a deactivation of the catalyst is used to measure a stability of the catalyst during the oxidative dehydration reactions.

(28) Referring now to FIG. 10 and FIG. 11, in one embodiment, no decrease in methanol conversion and/or DME selectivity is detected in oxidative dehydration reactions over a period of at least 60 hours, preferably at least 65 hours, preferably at least 70 hours, preferably at least 75 hours, preferably at least 80 hours, preferably at least 85 hours, preferably at least 90 hours, preferably at least 95 hours, preferably at least 100 hours, which indicates that the stability of the catalyst in the reaction conditions, without any catalyst deactivation.

(29) Further in some embodiments, the oxygen and methanol flow rate may be between 0.1 g/h to 0.7 g/h, preferably 0.2 g/h to 0.6 g/h, preferably 0.3 g/h to 0.5 g/h. In some embodiments, methanol or the mixture of methanol and oxygen is mixed with helium with a volumetric ratio of 1:1 to 1:9, preferably 1:2 to 1:6, preferably 1:3 to 1:4. In some embodiments, the methanol/helium or oxygen/methanol/helium gas mixture should be preheated prior to flowing into the reactor at a temperature of 125 C. to 200 C., preferably 130 C. to 170 C., preferably 140 C. to 160 C. In some implementations, the oxygen/methanol/helium flow rate is in the range of 20 mL/min to 75 mL/min, preferably 30 mL/min to 60 mL/min, preferably 40 mL/min to 50 mL/min. In some embodiments, a gas hourly space velocity (GHSV) of the reactor is 10,000 cm.sup.3 h.sup.1 g.sub.cat.sup.1 to 50,000 cm.sup.3 h.sup.1 g.sub.cat.sup.1, preferably 20,000 cm.sup.3 h.sup.1 g.sub.cat.sup.1 to 40,000 cm.sup.3 h.sup.1 g.sub.cat.sup.1. Gas hourly space velocity relates the flow rate of the mixed gas and the weight of the catalyst, and GHSV is measured at standard temperature and pressure. In some embodiments, the catalyst bed was preheated to a temperature from 200 C. to 300 C., preferably 225 C. to 275 C., preferably 240 C. to 250 C. The preheated catalyst bed may be ramped to a reaction temperature simultaneously with the reactor temperature at a ramping rate of 1 C./min to 10 C./min, preferably 3 C./min to 8 C./min, preferably 5 C./min to 6 C./min. In some embodiments, the pressure of the reactor is 0.5 atm to 1.5 atm, preferably 0.7 atm to 1.25 atm, more preferably 0.8 atm to 1.0 atm.

(30) The reactor may include, but is not limited to a fixed bed flow reactor, a moving bed reactor, or a fluidized bed reactor.

(31) According to a second aspect, the present disclosure relates to a method of manufacturing the Mn/CeO.sub.2 catalyst including mixing cerium oxide (CeO.sub.2) with a solution comprising a manganese salt and a solvent, evaporating the solvent to form a solid that includes manganese on a cerium oxide catalyst support. The manganese salt may include but is not limited to manganese bromide, manganese chloride, manganese carbonate, manganese fluoride, manganese iodide, manganese sulfate, and/or manganese nitrate.

(32) The term mixing as used herein preferably refers to a process that includes mechanical blending or agitation in a vessel by paddles, jets, or baffles. The mixing may occur sequentially or simultaneously. For example the manganese salt may first be dissolved or dispersed in solution, then followed by cerium oxide, or both manganese salt and cerium oxide may be combined in the solution simultaneously mixed. In some implementations, the solvent in which the manganese salt and/or the cerium oxide is prepared by dispersion or dissolution may be water, ethanol, methanol, acetonitrile, or a combination thereof. In some implementations, the solvent is at least 40% water, at least 30% water, at least 20% water, at least 10% water, or at least 1% water. In a preferred embodiment, the solvent is water and the manganese salt is manganese chloride tetra hydrate (i.e. MnCl.sub.2.4H.sub.2O). In addition, evaporating may be accomplished by a vacuum evaporation, preferably a rotary evaporation.

(33) The method further involves drying the solid at a temperature of 90 C. to 120 C., preferably around 100 C. for 2 hours to 5 hours, preferably about 3 hours. Besides, the method involves calcining the solid at a temperature of 450 C. to 550 C., preferably around 500 C. for 3 hours to 7 hours, preferably about 4 to 6 hours, more preferably about 5 hours to form the catalyst.

(34) In a preferred embodiment, the method further involves granulating the solid to form catalyst grains in the size range of 0.05 mm and 0.5 mm, preferably 0.06 to 0.3 mm, preferably 0.07 to 0.2 mm, preferably 0.08 to 0.1 mm.

(35) In another preferred embodiment, the grains may further be sieved to collect catalyst grains preferably with uniform shape and size. The sieving may include high frequency vibrating equipment, which drives a screen cloth to vibrate allowing material to be filtered that is smaller than a pore size of the screen; gyratory equipment, which gyrates in a circular motion at a near level plane at low angles to cause a material to shift back and forth and smaller material falls out of the box more easily than heavier material; or a trommel screens, which is a horizontal rotating drum with screen panels around the diameter of the drum through which material may be removed or captured based on size.

(36) The examples below are intended to further illustrate the method of producing dimethyl ether and the method of manufacturing the catalyst and are not intended to limit the scope of the claims.

Example 1

(37) The dehydration of methanol to DME over -Al.sub.2O.sub.3 and zeolite catalysts is carried out in the absence of oxygen whereas the present invention describes a method to produce DME by oxidative dehydration of methanol over a catalyst composed of manganese supported on cerium oxide (Mn/CeO.sub.2). The presently disclosed method employing the Mn/CeO.sub.2 catalyst requires minimal oxygen presence in the reaction mixture in order to produce DME from methanol with a high selectivity.

(38) The presently disclosed catalyst, which comprises manganese supported on low surface area CeO.sub.2 demonstrates a high catalytic activity and selectivity in the reaction of oxidative dehydration of methanol to DME. The interaction between Mn and CeO.sub.2 results in a change of the catalytic properties of the CeO.sub.2 as disclosed in data herein. Synergism was observed between deposited Mn and CeO.sub.2, which causes an increase in the catalyst efficiency towards producing the dimethyl ether. The result of this synergism was unexpected catalytic properties in the catalyst. Further, by combining a small amount of oxygen to the methanol feed stream, in the presence of Mn/CeO.sub.2 catalyst, methanol was transformed to DME with high selectivity relative to side products. The proposed catalyst composition for oxidative dehydration of methanol is different from the conventional catalysts and process for DME production.

Example 2Preparation of Mn/CeO2 Catalyst

(39) Manganese oxide was added to CeO.sub.2 (Acros, Belgium, 99.9%) by incipient wetness impregnation method. To prepare 5 g of 1 wt % Mn supported on CeO.sub.2 catalyst, 0.1876 g of Manganese Chloride Tetra Hydrate (MnCl.sub.2.4H.sub.2O, Techno Pharmchem HARYANA, India, 97%) was dissolved in 10 ml of deionized water at room temperature, resulting in a transparent solution. 5 g of CeO.sub.2 was then added to the MnCl.sub.2 aqueous solution. Water was then evaporated by using a rotary evaporator having the operating condition at 40 C. and 40-60 mbar. After completing the evaporation, the resulting powder was collected and dried in an oven at 100 C. for 3 h. The powder was then calcined in static air at 500 C. for 5 h. The desired temperature was attained by increasing the oven temperature from 25 C. to 500 C. having a ramping rate of 5 C. min.sup.1.

(40) The obtained powder material was tableted, and the tablets were grounded. A fraction of the grounded material with grain size between 0.08 and 0.1 mm was selected and used for catalytic activity and selectivity measurements.

(41) 3 wt % and 5 wt % Mn supported on CeO.sub.2 catalysts were also prepared by the same procedure as 1 wt % Mn/CeO.sub.2 catalyst.

(42) All catalysts are characterized as follows. Crystal structure of the prepared catalysts was characterized by X-ray diffraction. FIG. 1 shows XRD patterns of 1% Mn/CeO.sub.2, 3% Mn/CeO.sub.2, 5% Mn/CeO.sub.2 and pure CeO.sub.2 support.

(43) Specific surface area of the catalysts was measured by using N.sub.2 adsorption isotherms and Brunauer-Emmett-Teller (BET) analysis. Before the nitrogen adsorption, all the catalysts were degassed at 200 C. for 2 h under vacuum condition in order to remove adsorbates on the catalysts. The values of the surface area are shown in Table 2.

(44) TABLE-US-00002 TABLE 2 BET surface area of the catalysts Sample CeO.sub.2 support 1% Mn/CeO.sub.2 3% Mn/CeO.sub.2 5% Mn/CeO.sub.2 Surface area 10.0 9.6 8.6 8.0 (m.sup.2/g)

(45) Composition of the catalysts was analyzed by X-ray Fluorescence (XRF) as shown in Table 3. The nominal values (wt %) of Mn content are very close to the desired value of the preparation condition.

(46) TABLE-US-00003 TABLE 3 Composition of the catalysts (wt %) 1% Mn/CeO.sub.2 3% Mn/CeO.sub.2 5% Mn/CeO.sub.2 Ce 99.06 96.39 94.50 Mn 0.94 3.60 5.50

Example 3Oxidative Dehydration of Methanol Over 1% Mn/CeO2 Catalysts with Different O2/MeOH Ratios

(47) The process of the oxidative dehydration of methanol was carried out by using (PID Eng & Tech, System, Spain) with a fixed bed quartz reactor at atmospheric pressure in the temperature interval between 275 and 450 C. The reactor was charged with 0.1 g of catalyst with grain sizes between 0.08 to 0.1 mm. The catalyst bed was supported on the bed of quartz wool. The internal diameter of the quartz reactor was 4 mm, and the height of the catalyst bed was 7-8 mm. A K-type thermocouple was placed at the center of the catalyst bed to measure the reaction temperature.

(48) Liquid methanol flow was controlled by Bronkhorst High-Teck B.V. CEM system at 0.45 g h.sup.1. Oxygen (O.sub.2) flow was controlled at O.sub.2/MeOH ratio of 0.2, 0.3, and 0.5 (mol/mol) by a mass flow controller (Bronkhorst High-Teck B.V.).

(49) The required methanol and oxygen flow were mixed with helium in a mixing chamber heated at 150 C. The total flow of oxygen, methanol and inert He was 50 ml/min, and gas hourly space velocity (GHSV) was 30,000 cm.sup.3 h.sup.1 g.sub.cat.sup.1.

(50) Catalyst bed was preheated to 250 C. prior to introduce the reactants to the reactor. The reactor temperature was then increased to 275 C. at a ramping rate of 5 C./min. For each desired experimental condition, temperature (in between 275-450 C.) was held for 3 h to reach steady state prior to analyze the reaction products. The reactants and products were analyzed with an on-line gas chromatograph (HP, G1540A) equipped with TCD detectors. Molecular sieve 13X was used to separate O.sub.2 and CO, and Porapak QS was used to separate H.sub.2, CO.sub.2, H.sub.2O, CH.sub.2O (Formaldehyde), CH.sub.3OH and CH.sub.3OCH.sub.3 (Dimethyl ether).

(51) Conversion (%) of reactants and selectivity of products were calculated as follows in equations (1)-(7).

(52) $\begin{array}{cc}{\mathrm{CH}}_3\mathrm{OH}\mathrm{conversion}\left(\%\right)=\frac{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{in}}-\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{out}}}{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{in}}}100& \left(1\right)\\ O_2\mathrm{conversion}\left(\%\right)=\frac{\mathrm{mol}.\mathrm{of}{O}_{2\mathrm{in}}-\mathrm{mol}.\mathrm{of}{O}_{2\mathrm{out}}}{\mathrm{mol}.\mathrm{of}{O}_{2\mathrm{in}}}100& \left(2\right)\\ {\mathrm{CH}}_{2}O\mathrm{selectivity}\left(\%\right)=\frac{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_{2}O}{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{consumed}}}100& \left(3\right)\\ \mathrm{CO}\mathrm{selectivity}\left(\%\right)=\frac{\mathrm{mol}.\mathrm{of}\mathrm{CO}}{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{consumed}}}100& \left(4\right)\\ {\mathrm{CO}}_2\mathrm{selectivity}\left(\%\right)=\frac{\mathrm{mol}.\mathrm{of}{\mathrm{CO}}_2}{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{consumed}}100}& \left(5\right)\\ \mathrm{DME}\left({\mathrm{CH}}_3{\mathrm{OCH}}_3\right)\mathrm{selectivity}\left(\%\right)=\frac{2\left(\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OCH}}_3\right)}{\mathrm{mol}.\mathrm{of}{\mathrm{CH}}_3{\mathrm{OH}}_{\mathrm{consumed}}}100& \left(6\right)\\ \mathrm{DME}\mathrm{yield}\left(\%\right)={\mathrm{CH}}_3\mathrm{OH}\mathrm{conversion}\mathrm{DME}\mathrm{selectivity}/100& \left(7\right)\end{array}$

(53) FIG. 2, FIG. 3, FIG. 4 and FIG. 5 show MeOH conversion and selectivity obtained on 1% Mn/CeO.sub.2 at O.sub.2/MeOH ratio of 0, 0.2, 0.3 and 0.5, respectively. DME yields at each O.sub.2/MeOH ratio were compared as shown in FIG. 6.

(54) The 1% Mn/CeO.sub.2 catalyst showed quite small activity at the condition without O.sub.2 flow as shown in FIG. 2 and FIG. 6. Conversion measurements below 5% were a result of error in methanol flow rate. At the temperature range between 275 C. and 375 C., a small amount of DME was generated. When O.sub.2 was supplied with methanol at O.sub.2/MeOH ratio of 0.2, 0.3 and 0.5, a considerable amount of methanol was reacted and DME was obtained as main product at a temperature range between 275 and 325 C. DME yield was significantly increased with increase of the O.sub.2 flow as shown in FIG. 6. These results suggest that DME production over Mn/CeO.sub.2 catalyst needs oxygen and follows a different mechanism compared to the dehydration mechanism on -Al.sub.2O.sub.3 and on zeolites.

(55) 300 C. is an advantageous temperature because conversion at 300 C. is higher than that of 275 C. and DME selectivity at 300 C. is higher than that of at 325 C. Higher O.sub.2/MeOH ratio brought higher selectivity for CO.sub.2, resulting in relatively lower DME selectivity. Therefore, it was concluded that the reaction temperature at 300 C. and the O.sub.2/MeOH ratio at 0.2 for oxidative dehydration of methanol to DME, provided a usable level of DME yield.

Example 4Oxidative Dehydration of Methanol Over Mn/CeO2 Catalysts with Different Mn Contents

(56) Activity of 3% Mn/CeO.sub.2 and 5% Mn/CeO.sub.2 was tested at O.sub.2/Me ratio of 0.2, according to the same procedure as above in the preparation of Mn/CeO.sub.2 catalyst, as shown in FIG. 7 and FIG. 8. DME yields obtained over Mn/CeO.sub.2 catalysts with different Mn contents were compared as shown in FIG. 9. The increase of Mn content increases DME selectivity at middle temperature range (between 350 and 375 C.). However, at lower temperature such as 275 and 300 C., Mn content hardly influenced the activity and selectivity.

Example 5Stability Test of 1% and 3% Mn/CeO2 Catalysts at O2/MeOH Ratio of 0.2

(57) Methanol oxidative dehydration reaction over 1% and 3% Mn/CeO.sub.2 was isothermally performed at 300 C. and O.sub.2/MeOH ratio of 0.2 in order to examine the stability of the catalysts. As a result, both 1% Mn/CeO.sub.2 and 3% Mn/CeO.sub.2 catalysts didn't show any significant deactivation or any decrease in DME selectivity for a time period of 80 hours.

Example 6Oxidative Dehydration of Methanol Over Manganese Oxide

(58) Manganese oxide (MnOx) was synthesized by calcination of Manganese chloride (MnCl.sub.2.4H.sub.2O, Techno Pharmchem HARYANA, 97%) at 500 C. for 5 h according to the same calcination condition to prepare Mn/CeO.sub.2 catalysts. The activity of 100 mg of the synthesized MnOx was examined at O.sub.2/MeOH ratio of 0.5 according to the same procedure as Mn/CeO.sub.2 catalysts. As a result, MnOx showed much lower activity and DME yield at 300 C. than those of Mn/CeO.sub.2 catalysts as shown in FIG. 14 and FIG. 15. In addition, DME selectivity is also lower than Mn/CeO.sub.2 catalyst because of increased amount of formaldehyde production.

Example 7

(59) The analysis of the composition of the reaction mixture at the reactor output were done by gas chromatographic method by using the following chromatographic columns of a molecular sieve, Porapak, Tenax, hayeSep, and Chromosorb.

(60) FIG. 6 shows a comparison of data derived from FIG. 3, FIG. 4, and FIG. 5. The highest selectivity for DME and higher conversion of methanol were obtained at the reaction temperature of 300 C. and O.sub.2/MeOH ratio of 0.2 as depicted in FIG. 3. FIG. 7 and FIG. 8 depict data from exemplary reaction tests of 3% Mn/CeO.sub.2 and 5% Mn/CeO.sub.2 catalysts, respectively, at an oxygen/methanol ratio of 0.2. FIG. 9 depicts a comparison of data in FIG. 7 and FIG. 8.

(61) FIG. 10 and FIG. 11 depict data from two stability tests over 80 hours each. These stability tests demonstrated that Mn/CeO.sub.2 catalysts don't show any significant deactivation on their methanol conversion and selectivity for DME.

(62) FIG. 12 and FIG. 13 depict a comparison of a CeO.sub.2 support's catalytic efficiency in forming DME as compared to a 1% Mn/CeO.sub.2 catalyst's efficiency in forming DME. As shown in FIG. 13, the yield of DME over CeO.sub.2 is four to ten times smaller or five to eight times smaller than the yield obtained by using Mn/CeO.sub.2 at 300 C. to 375 C. The comparison clarifies that pure CeO.sub.2 support does not efficiently catalyze the DME production from methanol. Further, FIG. 14 and FIG. 15 depict data resulting from DME formation with a catalyst comprising only manganese oxide as compared to Mn/CeO.sub.2. The data in FIG. 14 and FIG. 15 show that pure manganese oxide does not exhibit any catalytic activity until a temperature of 325 C. When Mn is supported on CeO.sub.2, the obtained catalyst produces DME at temperatures as low as 275 C. Taking the data depicted in FIG. 13 and FIG. 15 together, the obtained figures are showing a proof that between Mn and CeO.sub.2 arises synergetic effect, that is exploited by the catalyst disclosed in the present invention and the method of producing DME as described herein. The yield of DME over Mn/CeO.sub.2 at temperatures of 275 C. to 375 C. is two to five times greater than expected DME yield obtained by sum DME yields of pure CeO.sub.2 and manganese oxide, which have no synergetic effect.

(63) DME yields obtained at 300 C. and various O.sub.2/MeOH ratios over CeO.sub.2, MnOx and Mn/CeO.sub.2 catalysts are organized in Table 4. The results clearly suggest that a synergistic effect between manganese oxide and ceria oxide significantly improves the catalytic activity to produce DME from methanol. The data suggests that O.sub.2 improves the production of DME with an Mn/CeO.sub.2 catalyst.

(64) TABLE-US-00004 TABLE 4 DME yields obtained at 300 C. and various O.sub.2/MeOH ratio. DME DME Sample O.sub.2/MeOH Yield (%) Selectivity (%) CeO.sub.2 0.5 3.2 MnOx 0.5 0.7 1% Mn/CeO.sub.2 0 5.0 0.5 20.1 83 0.3 16.8 85 0.2 19.2 86 3% Mn/CeO.sub.2 0.2 14.4 78 5% Mn/CeO.sub.2 0.2 17.6 84

(65) Presented herein is a catalyst to produce DME from Methanol with addition of oxygen; a synergistic effect between manganese oxide and cerium oxide has an important role for the reaction; Oxygen with the methanol may efficiently produce DME. The catalyst showed a high stability. 1% Mn/CeO.sub.2 and 3% Mn/CeO.sub.2 did not show any significant deactivation or decrease of DME selectivity during reaction carried out for longer than 60 h at 300 C. Oxygen may be included in the reactant stream to produce DME.