SILVER-BASED CATALYST FOR PRODUCTION OF ETHYLENE OXIDE

Abstract: This invention provides a catalyst comprising sodium and cesium as a cationic component and at least one of chlorine, bromine and fluorine as an anionic component in addition to silver which is a typical conventional catalyst component for the production of ethylene oxide by oxidation of ethylene. The catalyst of the invention gives ethylene oxide at an improved selectivity.

Description: SILVER-BASED CATALYST FOR PRODUCTION OF ETHYLENE OXIDE This invention relates to a process for the production of ethylene oxide by oxidizing ethylene, and to a catalyst therefor. It is based on the new discovery that a combination of sodium, cesium and a specified halogen ele- ment (chlorine, bromine and/or fluorine) with silver provides a catalyst having increased performance in the oxidation of ethylene. A silver catalyst is substantially the sole catalyst component used in the'industrial production of ethylene oxide by oxidation of ethylene with molecular oxygen. Silver alone, however, did not prove to be a perfect industrial catalyst, and efforts have been made to increase its performance by including various additives (for example, U. S. Patents Nos. 2238471, 2404438, 2671764 and 2799687). tinny of these efforts have been directed to the addition of alkali metals (for example, British Patent No. 1,413,251 and U. S. Patent No. 4,212,772). Usually, halogen compounds of these metals are excluded because they are a poison to silver. The present inventors have extensively made investigations about the effects of anionic components as well as alkali metals as cationic components. These investigations have led to the discovery that the use of the aforesaid specified halogen elements (to be referred to simply as a halogen element), previously believed to have a poisonous action, in combination with sodium and cesium unexpectedly gives a catalyst having greatly increased performance. SUMMARY OF THE INVENTION According to this invention, there is provided a catalyst for the production of ethylene oxide by oxidation of ethylene, comprising (A) silver, (B) (1) more than 1000 ppm (mg/kg of the catalyst) of sodium, and (2) cesium as a cationic component, and (C) at least one halogen element selected from the group consisting of chlorine, bromine and fluorine as an anionic component. In another aspect, there is provided a process for producing ethylene oxide, which comprises contacting ethylene and a gas containing molecular oxygen with the aforesaid catalyst at a temperature of 180 to 300 C and a --pressure of 1 to 35 kg/cm2. BRIEF DESCRIPTION OF THE DRAWING Figure 1 is a graph showing the effect of the sodium contents of the catalysts used in Examples 7 and 10 and Comparative Examples 6 to 9 on the selectivities of the catalysts and the reaction temperatures. DETAILED DESCRIPTION OF THE INVENTION In the preparation of the catalyst of this in vention, a sodium compound to be added is preferably in the form of sodium carbonate, sodium bicarbonate or sodium nitrate. It may, however, be in the form of a hydroxide, nitrite, sulfate, borate, silicate, phosphate, halide or carboxylate (e.g., sodium acetate or sodium oxalate), or a mixture of any of these compounds with sodium carbonate or sodium bicarbonate. A cesium compound to be added is preferably in the form of a chloride, bromide and/or fluoride depending upon the type of the halogen element to be added to the catalyst. It may be added in the form of any of water-soluble or water-insoluble compounds such as its hydroxide or salts such as the nitrate, nitrite, carbonate and sulfate. Sources of the halogen element may be sodium halides or cesium halides which are salts of halogens with sodium or cesium, or other salts such as BaCl2, NH4Cl, LiCl, KCl, RbCl, BaBr2, BaF2, KBr, KF, RbBr, RbF, LiBr and LiF. In any case, it is essential to add sodium, cesium and the halogen element as well as silver, and a combination of these gives a catalyst having greatly increased perfor mance. The amount of sodium added is more than 1000 ppm (rng/kg of catalyst) based on the catalyst. Preferably, it is from 1100 ppm to 1.50% by weight, more preferably 1200 ppm tio 1, by weight. Advantageously, the amount of sodium added ranges from 1300 ppm to 5000 ppm. Preferably, the amount of sodium is such that the atomic ratio of Na to At is not more than 0.58, especially not more than 0.45. When the amount of sodium is too large, both the activity and selectivity of the catalyst are reduced. Then it is too small, the dispersion of silver particles on a carrier is worse than that in the catalyst of this invention as observed by a scanning electron microscope; hence, the activity of the catalyst is low and a higher bath temperature is required in order to obtain the same activity, with the consequence that the effect of adding halogen is not fully produced. The suitable amount of cesium added is smaller than that of sodium. It is generally from 10 ppn to 0. 5P by weight, preferably from 15 ppm to 0. ld by weight, based on the catalyst. If the amount is too large, the activity of the catalyst is markedly decreased, and if it is too small, the effect of the halogen element is not fully produced. The suitable amount of the specified halogen element, i.e. chlorine, bromine and/or fluorine, used in the catalyst of this invention is from 5 ppra to 0. lp by weight, preferably from 7 ppm to 0. 07% by weight. The addition of too large an amount results in the exhibition of its poison in action and causes a drastic reduction in the performance of the catalyst. Thus, the characteristic feature of the invention is that the halogen element previously believed to have a poisoning action has been found to have an action of a performance improver by adding it in a very small amount in combination with sodium and cesium. The halogen elements may be used singly or as a mixture of two or three of them. In the catalyst of this invention, the cat ionic component is not limited to sodium and cesium, and a snall amount of a third component such as lithium, barium, rubidium, potassium and thallium may be added together. The above catalyst components are used in the form of a supported catalyst mainly from the standpoint of eco nony and active lifetime. A porous refractory material is used as a carrier. Desirably. the carrier has a BET surface area of 0.05 to 10 mê/g and an apparent porosity of at least 15%. A carrier composed of alpha-alumina as a main component (a so-called alundum carrier) is preferred. Deposition of sodium, cesium and the halogen element may be effected by dissolving or dispersing the aforesaid compounds of these ingredients in an aqueous solvent, impregnating a carrier with the resulting solution or dispersion, and drying the impregnated carrier under heat in the presence of a gas such as nitrogen or air. Sodium, cesium and the halogen element may be deposited simultaneously or separately in any desired stage of catalyst preparation in various modes. For example, similar effects can be obtained by performing the deposition before, during or after the impregnation of the silver compound. Deposition of silver can be carried out by dipping a carrier molded in a suitable form such as spheres, pellets or rings in an aqueous solution or dispersion prepared by dissolving or dispersing a silver compound such as silver oxalate, silver nitrate or silver lactate in water in the presence or absence of a solubilizing agent such as ethylenediamine, drying the impregnated carrier, and calcining it at a suitable temperature in a stream of a gas such as nitrogen, air or hydrogen. The kind of the gas and the temperature in the calcination are selected depending upon the kind of the silver salt, etc. The calcination temperature is usually 100 to 10000C, preferably 150 to 700 0C. The amount of silver supported in the catalyst is usually 1 to 25 by weight, preferably 3 to 20% by weight, based on the catalyst. The silver-based catalyst of this invention is used conveniently in the production of ethylene oxide by the oxidation of ethylene in the vapor phase with molecular oxygen. The reaction conditions for the oxidation of ethylene are known, and broadly described in the prior art literature. In the production of ethylene oxide in the presence of the silver-based catalyst of this invention, the reaction pressure is 1 to 35 kg/cmê, preferably 5 to 20 kg/cmê; the reaction temperature is 180 to 300 C, preferably 190 to 2600C; ethylene is used in an amount of 1 to 40% by volume, preferably 15 to 35 by volume; and oxygen is used in an amount of 1 to 20% by volume, preferably 5 to 10 by volume, diluted with a diluting agent such as methane and nitrogen, preferably methane, in an amount of 20 to 70 by volume, preferably 30 to 65% by volume. Oxygen may be supplied in the form of air or industrial oxygen. Preferably, a reaction inhibitor such as a halogenated hydrocarbon is added to the starting gaseous mixture. In particular, by adding several ppm to several ten ppm (by weight) of ethylene dichloride, vinyl chloride, etc. to the starting gas, the formation of hot spots in the catalyst can be prevented and the properties, especially the selectivity, of the catalyst can be greatly improved. The starting gaseous mixture is continuously introduced into a reactor filled with the catalyst. The resulting ethylene oxide is separated and recovered from the reaction mixture by using customary methods. The following examples illustrate the present invention more specifically. Example 1 AgNO3 (6.0 g) was dissolved in 100 ml of water, and separately, 3.4 g of potassium oxalate (K2C204wH20) was dissolved in water. The resulting solutions were mixed, and heated in a water bath to 600C to form a white precipitate of silver oxalate. Centrifugation and washing with distilled water were repeated to remove potassium from the precipitate. Separately, 6.6 ml of 1:1 mixture of ethylenediamine and water was prepared, and while cooling with ice, the silver oxalate precipitate was gradually dissolved in the mixture to prepare a silver solution. Thirty grams of an alpha-alumina carrier (SA-5161, a tradename for a product of Norton Company) was dipped in the silver solution, and after allowing the excess of the solution to flow out, was dried at 800C under reduced pressure in a rotary evaporator. The dried carrier was transferred into a calcination tube. The temperature was raised to 3000C in a stream of nitrogen over the course of 2 hours, and it was further calcined at this temperature for 2 hours to deposit silver on the carrier. Then, 2.0 g of Na CO and 0.04 g of CsCl were dissolved in 50 ml of a mixture of methanol and water (methanol content 30 by weight), and the silver-supported carrier was dipped in it. The excess of the solution was removed by filtration, and the impregnated carrier was dried at 110 0C for 2 hours in a stream of nitrogen gas to prepare a catalyst in accordance with this invention. The proportion of Ag supported was 8.oft by weight, and the proportions of Na, Cs and C1 supported were 0.35 by weight, 126 ppm, and 34 ppm, respectively. The catalyst was pulverized to a size of 9 to 28 mesh, and 10 g of the pulverized catalyst was filled in a steel reactor having an inside diameter of 20 mm. A gaseous mixture consisting of 30 by volume of ethylene, 8d by volume of oxygen, 2 ppm of vinyl chloride and the balance being methane was passed through the reactor at a pressure of 9 kg/cmê and an SV or 2000 hr-1. At a bath temperature (reaction temperature) of 2000C, an oxygen conversion of 35% and an ethylene oxide selectivity of 81.0% were obtained. At 207 C, the oxygen conversion was 61.0% and the ethylene oxide selectivity was 75. During the three-weekcontinuous operation, no change was noted in the performance of the catalyst. Example 2 Thirty grams of an alpha-alumina carrier (SA-5161) was dipped in 50 ml of an aqueous solution containing 2.0 g of sodium carbonate. The excess of the solution was removed by filtration, and the impregnated carrier was dried at 110 C for 2 hours in a stream of nitrogen gas to prepare a carrier impregnated with sodium carbonate. Silver was deposited on the carrier in the same way as in Example 1. The carrier was then dipped in a solution of 0.02 g of cesium chloride in 50 ml of a mixture of methanol and water (water content 0.3% by weight). The excess of the solution was removed, and the impregnated carrier was dried at 110 0C for 2 hours in a stream of nitrogen gas to prepare a catalyst in accordance with this invention. The proportion of Ag deposited was 8.0 by weight, and the proportions of Na, Cs and C1 deposited were 0.35° by weight, 63 ppm and 17 ppm, respectively. Ethylene was oxidized under the same conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 195 C, an oxygen conversion of 32% and an ethylene oxide selectvity of 80.0% were obtained. Comparative Example 1 The procedure of Example 1 was followed except that the amount of sodium carbonate was decreased to onetenth, and the amount of cesium chloride added was decreased to one-half. Thus, there was prepared a supported catalyst containing 8.0 by weight of Ag, 350 ppm of Na, 63 ppm of Cs and 17 ppm of C1. Ethylene was oxidized under the same conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 1950 C, an oxygen conversion of 23dye and an ethylene oxide selectivity of 79.5% were obtained. Example 3 Silver was deposited on a carrier (SA-5161) in the same way as in Example 1. The silver-supported carrier was then dipped in a solution of 2.0 g of sodium carbonate, 0.13 g of cesium nitrate and 0.014 g of sodium chloride in 50 ml of a mixture of methanol and water (methanol content 30 by weight). The excess of the solution was removed, and the impregnated carrier was dried at 1100C for 2 hours in a stream of nitrogen gas to prepare a catalyst in accordance with this invention. The proportion of Ag deposited was 8 by weight, and the proportions of Na, Cs and C1 deposited were 0.35 by weight, 315 ppm, and 34 ppm, respectively. Ethylene was oxidized under the same conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 210 C, an oxygen conversion of 34.5% and an ethylene oxide selectivity of 80.0% were obtained. Example 4 A supported catalyst containing 8.0 by weight of Ag, 0.22% by weight of Na, 126 ppm of Cs and 34 ppm of C1 was prepared in the same way as in Example 1 except that 2.0 g of sodium bicarbonate was used instead of sodium carbonate. Ethylene was oxidized under the same conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 215 C, an oxygen conversion of 30.0% and an ethylene oxide selectivity of 81.0s were obtained. Example 5 A supported catalyst containing 8.0% by weight of Ag, 0.23% by weight of Na, 126 ppm of Cs and 34 ppm of C1 was prepared in the same way as in Example 1 except that 2.0 g of sodium acetate was used instead of sodium carbonate. Ethylene was oxidized under the same conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 218 C, an oxygen conversion of 30.0% and an ethylene oxide selectivity of 81.0% were obtained. Example 6 A supported catalyst containing 8.0Z by weight of Ag, 0.24 by weight of Na, 126 ppm of Cs and 34 ppm of C1 was prepared in the same way as in Example 1 except that 2.0 g of sodium nitrate was used instead of sodium carbonate. Ethylene was oxidized under the same reaction conditions as in Example 1 using the resulting catalyst. At a reaction temperature of 2190C, an oxygen conversion of 34.0 and an ethylene oxide selectivity of 80.5X were obtained. Comparative Examples 2 to 5 Four different catalysts having the compositions shown in Table 1 were prepared in the same way as in Example 1, and tested under the same reaction conditions as in Example 1. The results together with those obtained in Example 1 are summarized in Table 1. It is seen from Table 1 that the catalyst of this invention shows higher selectivity. Table 1 EMI10.1 Reaction <tb> Raw <SEP> tempera- <SEP> Oxygen <tb> Composition <SEP> of <SEP> materials <SEP> ture <SEP> conversion <SEP> Selectivity <tb> Run <SEP> the <SEP> catalyst <SEP> added <SEP> ( C) <SEP> (%) <SEP> (%) <tb> Ag---Na---Cs---Cl <SEP> Na2CO3 <tb> Example <SEP> 1 <SEP> 8 <SEP> 0.35 <SEP> 126 <SEP> 34 <SEP> 207 <SEP> 61.0 <SEP> 75 <tb> CsCl <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag----Na <tb> 2 <SEP> 8 <SEP> 0.35 <SEP> Na2CO3 <SEP> 205 <SEP> 60.2 <SEP> 70.3 <tb> wt% <SEP> wt% <tb> Ag---Cs---Cl <tb> <SEP> 3 <SEP> 8 <SEP> 126 <SEP> 34 <SEP> CsCl <SEP> 228 <SEP> 60.0 <SEP> 68.0 <tb> wt% <SEP> ppm <SEP> ppm <tb> Ag---Na---Cs <SEP> Na2CO3 <tb> 4 <SEP> 8 <SEP> 0.35 <SEP> 126 <SEP> 200 <SEP> 58.5 <SEP> 67.7 <tb> wt% <SEP> wt% <SEP> ppm <SEP> CsNO3 <tb> Ag <SEP> Na <SEP> Cl <SEP> Na2CO3 <tb> 5 <SEP> 8 <SEP> 0.35 <SEP> 34 <SEP> 206 <SEP> 68.0 <SEP> 66.5 <tb> wt% <SEP> wt% <SEP> ppm <SEP> NaCl <tb> Example 7 Thirty grams of an alpha-alumina carrier (SA-5161) was dipped in 50 ml of an aqueous solution containing 2.2 g of sodium bicarbonate. The excess of the solution was removed by filtration, and the impregnated carrier was dried at 110 0C for 2 hours in a stream of nitrogen gas to prepare a sodium bicarbonate-impregnated carrier. Silver nitrate (6.0 g) was dissolved in 100 ml of water, and 3.4 g of potassium oxalate (K2C2O4H2O) was dissolved in 100 ml of water. The aqueous solutions were mixed, and heated to 60 0C in a water bath to form a white precipitate of silver oxalate. Centrifugation and washing with distilled water was repeated to remove potassium from the precipitate. Separately, 6.6 ml of a 1:1 mixture of ethylenediamine and water was prepared, and while cooling with ice, the precipitate of silver oxalate was gradually dissolved in the mixture to prepare a silver solution. The above carrier impregnated with sodium bicarbonate was dipped in the resulting silver solution. The excess of the solution was allowed to flow out, and the carrier was dried at 80 C under reduced pressure in a rotary evaporator. The dried carrier was transferred to a calcination tube and the temperature was raised to 3000C over the course of 2 hours. It was further calcined at this temperature for 1.5 hours. The calcined product was cooled, and dipped in 50 ml of a methanol/water mixture (water content 0.3% by weight) containing 0.043 g of cesium chloride. The excess of the solution was removed by filtration, and the impregnated carrier was dried at 1100C for 2 hours in a stream of nitrogen to prepare a catalyst in accordance with this invention which had the composition shown in Table 2. The catalyst was tested under the same reaction conditions as in Example 1. The results are shown in Table 2. Examples 8 to 10 In each run, a catalyst was prepared in the same was as in Example 7 except that the content of Na was changed as shown in Table 2. The resulting catalyst was tested in the same way as in Example 7. The results are shown in Table 2. Comparative Examples 6 to 8 In each run, a catalyst was prepared in the same way as in Example 7 except that the content of Na was outside the scope of the invention as shown in Table 2. The resulting catalyst was tested in the same way as in Example 7. The results are shown in Table 2. It is seen from Table 2 that the catalysts having an tia content outside the scope of the invention showed inferior selectivity to the catalyst of this invention. Comparative Example 9 A catalyst containing Cs and Na as cationic components in the same proportions as in Experiment 5C of Japanese Laid-open Patent Publication No. 127144/1980 and chlorine as an ionic component was repeated by the same catalyst preparing method using the same raw materials as in Example 7. The catalyst was tested under the same reaction conditions as in Example 7. The results are shown in Table 2. It is seen that the catalyst was inferior in selectivity to the catalyst of this invention. Table 2 EMI13.1 Composition <SEP> of <tb> the <SEP> catalyst <SEP> Results <SEP> of <SEP> the <SEP> reaction <tb> Oxygen <tb> Ag <SEP> Na <SEP> Cs <SEP> Cl <SEP> Temperature <SEP> conversion <SEP> Selectivity <tb> (wt%) <SEP> (ppm) <SEP> (ppm) <SEP> (ppm) <SEP> ( C) <SEP> (%) <SEP> (%) <tb> 7 <SEP> 8.4 <SEP> 2500 <SEP> 160 <SEP> 42 <SEP> 219 <SEP> 40 <SEP> 80.8 <tb> <SEP> 8 <SEP> 8.4 <SEP> 1380 <SEP> 160 <SEP> 42 <SEP> 223 <SEP> 40 <SEP> 80.2 <tb> 9 <SEP> 8.9 <SEP> 5000 <SEP> 150 <SEP> 40 <SEP> 218 <SEP> 40 <SEP> 80.5 <tb> 10 <SEP> 8.4 <SEP> 13000 <SEP> 160 <SEP> 42 <SEP> 218 <SEP> 40 <SEP> 79.8 <tb> 6 <SEP> 8.3 <SEP> 0 <SEP> 160 <SEP> 42 <SEP> 217 <SEP> 40 <SEP> 77.2 <tb> 7 <SEP> 8.4 <SEP> 100 <SEP> 160 <SEP> 42 <SEP> 226 <SEP> 40 <SEP> 78.1 <tb> 8 <SEP> 8.4 <SEP> 800 <SEP> 160 <SEP> 42 <SEP> 224 <SEP> 40 <SEP> 78.9 <tb> 9 <SEP> 8.4 <SEP> 100 <SEP> 50 <SEP> 13 <SEP> 218 <SEP> 40 <SEP> 76.0 <tb> The effect of the Na contents of the catalysts shown in Table 2 on the selectivity and reaction temperature plotted on a graph shown in Figure 1, in which the axis of abscissas represents the Na content (ppm) on a logarithmXc scale and the axes of ordinates, the left and right ones, represent the selectivity ( ) for ethylene oxide and the reaction temperature (OC), respectively. In Figure 1, the curve A represents the selectivity; the curve B, the reaction temperature corresponding to the curve A; and the black points C and D, the selectivity obtained under the conditions of Comparative Example 9 and the reaction temperature employed. It is seen from the results shown by the curves A and B of Figure I that when the amount of sodium added exceeds 1000 ppm, especially about 1100 ppm, based on the catalyst, the catalyst of this invention gives a markedly increased selectivity for ethylene oxide at relatively low reaction temperatures. It is also seen from Figure 1 that when the amount of sodium added is within the range of 1200 ppm to 1 by weight, ethylene oxide can be produced at a high selectivity at low temperatures, and therefore amounts of sodium within this range are preferred. Example 11 Thirty grams of an alpha-alumina carrier (SA 5561) was dipped in 50 nl of an aqueous solution containing 2.0 g or sudium carbonate. The excess of the solution was removed by filtration. and the dipped carrier was dried at 110 C for 2 hours in a stream of nitrogen gas to prepare a sodium carbonate-inpregnated carrier. Silver nitrate (6.0 g) and 3.4 g of potassium oxalate (K2C2O4.H2O) were each dissolved in 100 ml of water. The resulting aqueous solutions were then mixed, and heated in a water bath at 60 C to obtain a white precipitate of silver oxalate. Potassium was rernoved from the precipitate by repeating centrifugation and washing with distilled water. Separately, 6.6 ml of a 1:1 mixture of ethylenediamine and water was prepared, and with ice cooling, the silver oxalate precipitate was gradually dissolved in the mixture to prepare a silver solution. The above carrier was dipped in the resulting solution. The excess of the solution was allowed to flow out, and the dipped carrier was dried at 800C under reduced pressure in a rotary evaporator. The dried carrier was transferred to a calcination tube, and the temperature was raised in a nitrogen stream over the course of 2 hours to 3000C at which it was calcined for an additional 2 hours. The calcined product was cooled, and dipped in 50 ml of a methanol/water mixture (water content 0.3% by weight) containing 0.05 g of CsBr. The excess of the solution was removed by filtration, and the dipped product was dried at 1105 C for 2 hours in a stream of nitrogen gas to prepare a supported catalyst of this invention containing 8 by weight of Ag, 0.35 by weight of Na, 126 ppm of Cs and 76 ppm of Br. The resulting catalyst was pulverized to a size of 9 to 28 nesh, and 10 g of the pulverized catalyst was filled in a steel reaction tube having an inside diameter of 20 mm. A gaseous mixture consisting of 30% by volume ethylene, 8% by volume of oxygen, 2 ppm of vinyl chloride and the balance being methane was passed through the reaction tube at a pressure of 9 kg/cmê and an SV of 2000-1. At a bath temperature of 213 0C, an oxygen conversion of 30 and an ethylene oxide selectivity of 81 d were obtained. During the 3-week operating period, no change in the performance of the catalyst was noted. Example 12 A supported catalyst containing 8.0s of Ag, 0.35 by weight of Na, 126 ppm of Cs and 18 ppm of F was prepared in the same way as in Example 11 except that 0.036 g of CsF was used instead of CsBr. The catalyst was tested under the same reaction conditions as in Example 11. At a reaction temperature of 2160C, the results shown in Table 3 were obtained. Example 13 A supported catalyst containing 7.2% by weight of Ag, 0.19 by weight of Na, 126 ppm of Cs and 76 ppm of Br was prepared in the same way as in Example 11 except that 2.0 g of sodium bicarbonate was used instead of sodium carbonate. The catalyst was tested under the same reaction conditions as in Example 11. At a reaction temperature of 217 C, the results shown in Table 3 were obtained. Example 14 A supported catalyst containing 8.0% by weight of Ag, 0.35% by weight of Na, 126 ppm of Cs, 37 ppm of K and 18 ppm of F was prepared in the same way as in Example 11 except that 0.014 g of KF and o.o46 g of CsNO3 were used instead of CsBr. The catalyst was tested under the same conditions as in Example 11. At a reaction temperature of 2170C, the results shown in Table 3 were obtained. Table 3 EMI17.1 Raw <SEP> Oxygen <tb> Composition <SEP> of <SEP> materials <SEP> conversion <SEP> Selectivity <tb> Runs <SEP> the <SEP> catalyst <SEP> added <SEP> (%) <SEP> (%) <tb> Ag----Na----Cs----F <SEP> Na2CO3 <tb> Example <SEP> 12 <SEP> 8.0 <SEP> 0.35 <SEP> 126 <SEP> 18 <SEP> CsF <SEP> 50 <SEP> 79 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag-----Na <tb> 10 <SEP> 8.0 <SEP> 0.35 <SEP> Na2CO3 <SEP> 50 <SEP> 72.8 <tb> wt% <SEP> wt% <tb> Ag---Cs---Br <tb> 11 <SEP> 8.0 <SEP> 126 <SEP> 76 <SEP> CsBr <SEP> 50 <SEP> 70.3 <tb> wt% <SEP> ppm <SEP> ppm <tb> Ag---Na---Cs---I <SEP> Na2CO3 <tb> <SEP> 12 <SEP> 8.0 <SEP> 0.35 <SEP> 126 <SEP> 120 <SEP> CsI <SEP> 50 <SEP> 60 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag---Na---Cs---Br <SEP> Na2CO3 <tb> 13 <SEP> 8.0 <SEP> 0.01 <SEP> 50 <SEP> 30 <SEP> CsBr <SEP> 50 <SEP> 74.5 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag---Na---Cs---F <SEP> Na2CO3 <tb> 14 <SEP> 8.0 <SEP> 0.01 <SEP> 50 <SEP> 7 <SEP> CsF <SEP> 50 <SEP> 74.0 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Comparative Examples 10 to 14 Five different catalysts having the compositions shown in Table 4 ere prepared in the same way as in Example 11. These catalysts were each tested under the same reaction conditions as in Example 11 except that the oxygen conversion was set at 50 . The results are shown in Table 4 together with those obtained in Example 12. It is seen that the selectivity of the catalyst of this invention is superior. Table 4 EMI19.1 Raw <SEP> Oxygen <tb> Composition <SEP> of <SEP> materials <SEP> conversion <SEP> Selectivity <tb> Example <SEP> the <SEP> catalyst <SEP> added <SEP> (%) <SEP> (%) <tb> Ag----Na---Cs---Br <SEP> Na2CO3 <tb> 11 <SEP> 8.0 <SEP> 0.35 <SEP> 126 <SEP> 76 <SEP> CsBr <SEP> 30 <SEP> 81 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag----Na---Cs---F <SEP> Na2CO3 <tb> 12 <SEP> 8.0 <SEP> 0.35 <SEP> 126 <SEP> 18 <SEP> CsF <SEP> 30 <SEP> 82 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag----Na---Cs---Br <SEP> Na2CO3 <tb> 13 <SEP> 7.2 <SEP> 0.19 <SEP> 126 <SEP> 76 <SEP> CsBr <SEP> 30 <SEP> 82 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <tb> Ag----Na----Cs---K----F <SEP> Na2CO3 <tb> 14 <SEP> 8.0 <SEP> 0.35 <SEP> 126 <SEP> 37 <SEP> 18 <SEP> KF <SEP> 30 <SEP> 81 <tb> wt% <SEP> wt% <SEP> ppm <SEP> ppm <SEP> ppm <SEP> CsNO3 <tb> Example 15 A supported catalyst comprising 8.4 by weight of As, 2500 ppm of Na, 160 ppm of Cs, 21 ppm of C1 and 47 ppm of Br was prepared in the same way as in Example 7, and tested under the same reaction conditions as in Example 7. At a reaction temperature of 2200C, an oxygen conversion of 40% and a selectivity of 81.1 were obtained. Example 16 A supported catalyst comprising 8.4% by weight of Ag, 2500 ppm of Na, 160 ppm of Cs, 47 ppm of Br and 11 ppm of w was prepared in the same way as in Example 7, and tested under the same reaction conditions as in Example 7. At a reaction temperature of 216 C, an oxygen conversion of 30 and a selectivity of 82.5% were obtained.

Claims: WHAT WE CLAItI IS 1 A catalyst for the production of ethylene oxide by oxidation of ethylene, said catalyst comprising (A) silver, (B) (1) sodium in an amount of more than 1000 ppm (n.g/kg of catalyst) based on the catalyst and (2) cesium as a cationic component, and (C) at least one halogen element selected from the group consisting of chlorine, bromine and fluorine as an anionic component. 2. The catalyst of claim 1 wherein the amount of sodium is in the range of from 1100 ppm to 1.50= by weight based on the catalyst. 3. The catalyst or claim 1 wherein the amount of sodium is in the range of from 1200 ppm to 1 by weight based on the catalyst. 4. The catalyst of any one of claims 1 to 3 wherein the amount of cesium is in the range of from 10 ppm to 0.5 by weight based on the catalyst. 5. The catalyst of any one of claims 1 to 4 wherein the amount of the halogen elernent is in the range of from 5 ppm to 0.1 by weight based on the catalyst. 6. The catalyst of any one of claims 1 to 5 wherein silver, sodium, cesium and halogen element as catalyst ingredients are suported on a porous refractory carrier having a surface area of 0.05 to 10 mê/g and an apparent porosity of at least 15. 7. A process for the production of ethylene oxide, which comprises contacting ethylene and a gas containing molecular oxygen at a temperature of 180 to 3000C and a pressure of 1 to 35 kg/cm2 with a catalyst comprising (A) silver, (B) (1) sodium on an amount of more than 1000 ppm (mg/kg of catalyst) based on the catalyst, and (2) cesium as a cationic component, and (C) at least one halogen element selected from the group consisting of chlorine, bromine and fluorine as an anionic component.

Inventors: AYAME, AKIMI, NOJIRI, NAOHIRO, SAKAI, YUKIO
Applicants: MITSUBISHI PETROCHEMICAL CO., LTD.
Application year: 1982
Main classification: B01J23
IPC codes: B01J23, C07D301