Simultaneous production of morpholine and 2-(2-aminoalkoxy)alkanols

Abstract: A morpholine and a 2-(2-aminoalkoxy) alkanol e.g. 2-(2-aminoethoxy) ethanol may be obtained by reacting a dialkylene glycol e.g. in which each R is independently hydrogen or alkyl with ammonia in the presence of added hydrogen over a nickel-chromium oxide catalyst, employed in combination with an oxide-supported nickel catalyst. Use of the oxide-supported nickel catalyst suppresses formation of carbon dioxide.

Description: This invention relates to the practice of making morpholine from diethylene glycol by an amination reaction. More particularly this invention relates to the use of novel nickel-based, dual-catalyst systems for the selective amination of dialkylene glycols such as diethylene glycol (DEG) to corresponding morpholine derivatives and corresponding aminoalkoxy alkanols, such as 2-(2-aminoethoxy)ethanol (DGA), wherein the coproduction of CO₂ is significantly suppressed. Surprisingly, it has been found that only certain combinations of nickel-based dual catalyst systems are effective in suppressing CO₂ formation during this reaction. The practice of making morpholine plus DGA from diethylene glycol and ammonia over an amination catalyst is well-known in the art (see, for example, US-A-3151112). It is also known from US-A-4508896 to carry out such a reaction in the presence of a catalyst comprising oxides of nickel, copper and chromium. The reaction is generally run in an aqueous environment. The indication is that better productivity could be obtained using an anhydrous feed, since water acts as a diluent and takes up space in the reactor. Whether run under aqueous or anhydrous feed conditions, there are two principal gaseous by-products, methane and carbon dioxide. Under aqueous conditions most of the CO₂ is absorbed into the H₂O. Under anhydrous feed conditions, even though water is a reaction by-product (e.g. see Equations 1 and 2), the CO₂ will readily react with the excess ammonia to form ammonium bicarbonate and/or ammonium carbamate, both of which will in the absence of adequate water diluent, form solids which precipitate downstream of the amination reactor, in the heat exchanger, etc., causing additional unit maintenance costs and engineering problems. It would be extremely advantageous if it were possible to operate a morpholine/DGA process using anhydrous diethylene glycol/ammonia feed in such a fashion that CO₂ by-product formation was lowered to below, or close to, threshold levels (i.e. <50 ppm). Such a condition might be achieved by converting the CO₂ into methane (Equation 3), possibly by introducing a methanation catalyst into the process unit, downstream of the diethylene glycol amination step. Particularly useful would be a methanation catalyst that: a) Lowers CO₂ concentration in the morpholine/DGA product effluent to threshold levels. b) Is stable in the high pH, amine, environment of the morpholine DGA/product effluent. c) Remains an active methanation catalyst in said environment for extended periods, particularly at the temperature of DEG amination (190-250°C) d) Does not convert the desired morpholine and DGA into unwanted by-products, as a result of catalyzing secondary reactions in the crude product effluent. CO₂ + 4H₂ → CH₄ + 2H₂O No art has been found dealing with a provision for converting by-product CO₂ into methane when the CO₂ is present in an amination product effluent, particularly where the CO₂ is present in a morpholine DGA product mixture resulting from the amination of diethylene glycol (DEG) with ammonia. It is known that carbon dioxide can be converted into methane by reduction with four moles of hydrogen (Equation 3). This is called the "Sabatier reaction". The mechanism for the reaction is not clear and early researchers assumed that the reaction occurred in stages, but Bardet and Trambouze reported in C.R Hebd. Seances. Acad. Sci., Ser. C. 288 (1979). 101, that it appeared CO₂ methanation had its own mechanism, distinct from CO methanation, and that CO₂ methanation occurs faster and at lower temperatures than methanation of CO. Heterogeneous catalysts have proven best for this process. see "Carbon Dioxide Activation by Metal Complexes," by A. Behr, Chapter 4, p. 85 (1988). The mechanism for hydrogenation of CO₂ on nickel is discussed in an article by G. D. Weatherbee, et al. in J. Catal., 77 , 460-472 (1982). The rate of CO₂ hydrogenation was measured as a function of H₂ and CO₂ partial pressures at 500-600 K, 140 kPa and 30,000-90,000h⁻¹. The data indicated the rate of CO₂ hydrogenation is moderately dependent on CO₂ and H₂ concentrations at low partial pressures, but essentially concentration-independent at high partial pressures. Under typical conditions, CO was observed as a product of the reaction at levels determined by quasi-equilibrium between surface and gas phase CO species. Addition of CO to the reactants above this equilibrium level caused a significant decrease in the rate of CO₂ hydrogenation, apparently as a result of product inhibition. These authors set forth the following table which in their view summarized the mechanism for CO₂ hydrogenation and accounted for the observations of this study and other recent studies. The authors also noted that kinetic studies of methanation in their laboratory provided evidence that there are several mechanistic regimes, involving different rate controlling steps, the importance of which depends mainly on temperature. The authors proposed that at moderate reaction temperatures (525-575 K), CO dissociation appeared to be rate controlling, while hydrogenation of carbon apparently controlled at higher reaction temperatures (>575 K). This suggested that CO and CO₂ methanation rates on nickel are both controlled by CO dissociation at moderate reaction temperatures (525-575 K), a hypothesis consistent with the observation of nearly identical specific reaction rates in CO₂ and CO methanation on Ni/SiO₂. The authors further proposed that it is possible for the two reactions to follow similar paths and still have different rate determining steps. CO₂ Methanation catalysts are discussed in an article by A.D. Tomsett, et al. in Applied Catal. 26 391 (1986). This investigation was made in the context of identifying highly active catalysts suitable for the second of two stages in a process for the conversion of syngas into substitute natural gas. It was found that supported Ni-La₂O₃-Ru catalysts are effective for CO₂ methanation. These catalysts provided high activity and complete conversion of CO₂ into methane at a temperature as low as 250°C. It was concluded that the high activity of the Ni-La₂O₃-Ru catalysts is mainly ascribable to the larger number of active sites. It is known that methanation reactions are the reverse of reforming reactions. The methanation reactions are exothermic and therefore, since a methanator typically operates at a temperature of 300-400°C, the CO and CO₂ at the inlet should be carefully monitored to avoid damage to catalyst and vessel, see Kirk-Othmer, Encyclopedia of Chem.Tech., 3rd Edition, Vol. 2, p. 494. Related art includes an investigation discussed in an article by H. Baussart, et al. in J. Chem. Soc. Faraday Trans. I, 83 , 1711 (1987). Here Co, K and Cu, as components of catalysts, were investigated for the specific roles each played in the hydrogenation of CO₂. The results indicated, inter alia that a steady state was reached after ca. 30 hours of activation. It was found that the presence of cobalt favoured the formation of alkanes, and that the presence of potassium favoured the formation of CO resulting from a reverse water-gas shift reaction (CO₂ + H₂ →CO + H₂O). Further, it appeared the presence of copper in Russell catalysts increased the activity and the selectivity for CH₄ and reduced the number of products. There is a report on results of investigations into potassium-promoted nickel catalysts by T.K. Campbell, et al. in Applied Catal., 50 , 189 (1989). It was found potassium did not increase selectivity for higher hydrocarbons or olefins, but it changed the CH₄/CO product distribution. It was also found that potassium did not change CO₂ methanation mechanism, and the mechanism appeared to be quite similar to that for CO hydrogenation. This paper presented steady-state kinetic data for CO₂ hydrogenation on Ni/SiO₂ and Ni/SiO₂-Al₂O₃ catalysts for a range of potassium concentrates. It was reported that hydrogenation reactions of CO₂ and CO on potassium-promoted nickel catalysts are similar: The activities and selectivities depend significantly on the support. The rate of methanation on Ni/SiO₂ decreases exponentially for both reactions with potassium addition. The rate of methanation on Ni/SiO₂-Al₂O₃ initially increases for both reactions with potassium addition. US-A-4508896 describes a process for simultaneously producing a 2-(2-aminoalkoxy)alkanol compound and a morpholine compound by contacting an oxydialkanol with ammonia in the presence of a hydrogenation/dehydrogenation catalyst which comprised 60-85 mole% of nickel, 14-37 mole % of copper and 1-6 mole % of chromium, calculated on an oxide-free basis. This work does not address the problem of a methanation catalyst, CO₂ production and its effect in lowering productivity JP-A-58-225078 discloses the production of morpholine by reacting diethylene glycol and ammonia on a catalyst comprising nickel, copper, chromium and rhenium, in specific ratios, on an α-alumina carrier, the catalyst having been prepared by impregnation of the carrier, followed by hydrogenation. Preoxidized rhodium was studied as a catalyst for methanation of carbon monoxide in an article by A. Amariglio, et al. in J. Catal., 81 247 (1983). The authors confirmed that, according to their experiments, preoxidation of Rh caused a dramatic enhancement of its activity in the methanation of CO₂. They estimated preoxidation allowed the rate to be increased by a factor of 100, at the lowest estimate. The authors also concluded that the deactivation, observed upon prolonged exposures to H₂, must be ascribed to depletion of the preincorporated oxygen. From the art available, it is evident that there are many factors and multiple variables involved in the methanation of CO₂, such that it would be difficult to identify a catalyst which would promote methanation at low temperatures (<250°C) and high pH within a dual catalyst system where the conditions are geared toward a primary reaction, such as amination. It would constitute a distinct advance in the art if a catalyst system were available whereby CO₂ formation could be suppressed during morpholine/DGA amine processing by amination of DEG under anhydrous conditions. It has been discovered that the choice of methanation catalyst is very important. Many known methanation catalysts cannot be used in this fashion because of certain critical factors, particularly those outlined above. Unexpectedly it has been discovered that a dual catalyst system comprising a nickel-copper-chromium oxide in conjunction with an oxide-supported nickel catalyst is very effective for selective amination of DEG to morpholine plus DGA while at the same time significantly suppressing the coproduction of CO₂. This invention relates to an improved process for simultaneously producing a morpholine and a 2-(2-aminoalkoxy) alkanol by reacting a dialkylene glycol with ammonia in the presence of added hydrogen over a nickel-copper-chromium oxide catalyst. According to the improvement, said catalyst is employed in combination with an oxide-supported nickel catalyst, both catalysts being defined below. Preferably the dialkylene glycol has the formula in which each R is independently hydrogen or alkyl. Preferably the reaction is carried out at a temperature of 150 to 300°C, and a pressure of 1.45 to 34.6 MPa (200 to 5000 psig) under anhydrous feed conditions and in the presence of a substantial quantity of hydrogen. According to the preferred embodiment, oxydiethanol, also known as diethylene glycol, is contacted with ammonia and hydrogen in the presence of a catalytically effective amount of a dual catalyst system comprising an amination/hydrogenation/dehydrogenation catalyst and the oxide-supported nickel catalyst. The amination/hydrogenation/dehydrogenation catalyst is an oxide of 60 to 85 mole % of nickel, 14 to 37 mole % of copper and 1 to 6 mole % of chromium. The reaction is preferably a continuous process and preferably the molar ratio of ammonia to oxydiethanol is from 4:1 to 8:1. Preferably, the space velocities of the liquid feed material, i.e. ammonia and oxydiethanol, are from 1 to 6g of liquid feed per hour per cm³ of catalyst. The recovered reaction product, consisting primarily of DGA and morpholine, is recovered from the resultant crude reaction product by conventional means, such as distillation or extraction. The oxydialkanol compound that can be utilized in practicing the instant invention can have the general formula wherein each R is, hydrogen or alkyl for example, methyl or ethyl. The examples demonstrate the effectiveness of oxydiethanol or diethylene glycol. The nickel-copper-chromium oxide catalyst for amination of diethylene glycol which may be employed in the invention may generally be characterized as an amination catalyst or as an amination/hydrogenation/dehydrogenation catalyst. Examples of other catalyst components include copper, cobalt, manganese, molybdenum, palladium, platinum, rhodium, oxides of such metals and mixtures thereof. The catalyst comprises 60-85 mole % of nickel, 14-37 mole % of copper and 1-6 mole % of chromium with the preferred proportions being 72-78 mole % of nickel, 20-25 mole % of copper and 1-3 mole % of chromium. A greatly preferred hydrogenation catalyst is one which the active components comprise about 75 mole % of nickel, 23 mole % of copper and 2 mole % of chromium, in the form of an oxide. A commercially available amination/hydrogenation catalyst fitting this description is Engelhard Ni-2715 T 3/16" (4.8 mm). As mentioned above, only certain combinations of nickel-based dual catalyst systems are effective in suppressing CO₂ formation during morpholine production, and it has been surprisingly discovered in the instant invention that an effective methanation catalyst in combination with the nickel-copper-chromium oxide catalyst, is an oxide-supported nickel catalyst. Said oxide supports is selected from the oxides of the Group II, III and IV elements. The preferred supports include magnesia, allumina, silica, zirconia and titania, as well as mixtures thereof. The most preferred support is alumina. The nickel may be added to said support by any of the usual methods, and said formulated catalyst comprises from 10 to 80 wt% of nickel. The preferred nickel loading is 40 to 60 wt % and the preferred catalyst formulation comprises 40-60 wt % nickel-on-alumina. Suitable commercially-available catalysts include Engelhard D-4132 and Calsicat Catalysts E331, E475 and E217. Said combination of nickel-based dual catalysts may be used in any proportions, except that preferably the nickel-copper-chromium oxide catalyst should contact the diethylene glycol/ammonia feed first, in order to achieve the desired amination (Equations 1 and 2), then after the desired DEG conversion is achieved, the reactant product should contact the oxide-supported nickel catalyst in order to lower significantly the CO₂ effluent concentration (through Reaction 3). A particularly effective ratio of nickel-copper-chromium oxide catalyst to oxide-supported nickel catalyst is in the range 1:1 to 10:1 by volume. The accompanying examples illustrate such a ratio range. A particularly preferred dual nickel catalyst combination is Engelhard Ni-2715 T 3/16" and Engelhard D-4132 E 1/16". The ratio of reactant, i.e. the ratio of ammonia to oxydiethanol, or other oxydialkanol used in this process is from 1:1 to 10:1, although a molar excess of ammonia produces increased yields of the morpholine product. Optimum yields are obtained when the molar ratio of ammonia to oxydiethanol is about 6:1. The space velocities of the feed, namely, the ammonia and the glycol, may be from 1 to 6 grams of liquid feed/hour/milliliter of catalyst. As noted above, the temperature is from 150 to 300°C; the preferred range is from 200 to 250°C, depending upon the reactant ratios utilized. Those skilled in the art will realize that an outstanding advantage of the instant process resides in the fact that the relative yields of morpholine and DGA can be varied by a slight variation of reaction conditions while the production rate of the combined products remains high. Thus, one can achieve a substantial yield of 2-(2-aminoethoxy) ethanol while simultaneously maintaining morpholine production rates comparable to or better than those obtained by previously known methods. The process should be carried out in a reducing atmosphere, using hydrogen for commercial operations. Although small amounts of hydrogen are present during the reaction, from the catalyst materials and as a by-product, it is preferred that hydrogen be added in the feed system in order to achieve CO₂ methanation (Equation 3) and to maintain catalytic activity. The quantity of hydrogen necessary for the practice of this invention is generally from 0.1 to 1000 liters (1) per lb (0.454Kg) of DEG converted, the preferred range is from 10 to 200 liters and H₂ per lb (0.454Kg) of DEG converted. Such a ratio is illustrated in the accompanying examples. The quantity of CO₂ produced in this morpholine/DGA process is normally measured in terms of parts per million (ppm) in the effluent product, and is expressed in terms of Kg of CO₂ generated per 100M Kg of DEG converted. The accompanying examples illustrate the following: 1) In Example I, the generation of morpholine plus DGA is demonstrated using a dual, nickel-based, catalyst system comprising a nickel-coppper-chromium oxide catalyst (Engelhard Ni-2715 T 3/16" [4.8mm]) in combination with a nickel-on-alumina (Engelhard D-4132 E 1/16" [1.6mm]) to achieve: 85% DEG conversion of 220°C with 133 Kg Co₂ per 100 Kg DEG converted. 2. In Example 3, the same catalyst combination at a higher hydrogen flow rate of 90 1/hr provided: 77% DEG conversion at 215°C with an average of just 35 Kg Co₂ per 100M Kg DEG converted. 3. By comparison, in comparative Example A, using only Ni-2715 T 3/16" [4.8mm]. 82% DEG conversion at 220°C gave 499 Kg CO₂ per 100M Kg converted. We conclude that: a) Comparing Examples 1 and 4, the CO₂ made using the nickel dual catalyst system is cut from 499 to 133 Kg per 100M Kg DEG converted, a factor of 3.75. b) Comparing Examples 3 and 4, the CO₂ made using the nickel dual catalyst system and a higher hydrogen flow is cut from 499 to an average of 34 Kg per 100M Kg DEG converted, a factor of ca. 15. 4) Other oxide-supported nickel catalysts, in combination with Ni-2715 T 3/16" [4.8mm] are effective in lowering the CO₂ effluent production to the range of 12-41 Kg CO₂/100M Kg DEG converted (see Examples 5-7), while a nickel-copper-chromium on alumina catalyst was generally ineffective (see Comparative Example B). 5. The Ni-2715 T 3/16" + D4132 E 1/16" combination is effective in substantially lowering CO₂ production over 500 hours of operation, where the volume ratio of the two catalysts is ca. 2.7:1 (Example 8). Example 1 A 550 cc capacity plug-flow reactor fitted with heating, cooling and pressure control devices, and constructed of stainless steel, was charged with a combination of 400cc of pelleted nickel-copper-chromium oxide catalyst (in which the active components were 71.2 wt% Ni, 12.3 wt% Cu and 73.3% reduced Ni) and 150cc of extruded nickel-on-alumina catalyst (47.5% Ni). The pelleted nickel-copper-chromium oxide catalyst was placed in the bottom section of the reactor and the nickel-on-alumina at the top. Diethylene glycol (0.54Kg/h), ammonia (1.09Kg/h) and hydrogen (35 liters/h) were fed separately to the reactor system from the bottom of the reactor, in an upflow mode, through the catalyst bed of the reactor. The reactor effluent was cooled and depressurized, and the gaseous and liquid products were analyzed. After a 48-hour prerun period, to establish steady state conditions, the performance of the dual-catalyst system was tested at a series of operating temperatures (210-240°C) while maintaining a reactor back-pressure 15.27MPa (2200 psi). Data and results from the run are summarized in Table I. It may be noted that in this run: At an operating temperature of 210°C, the DEG conversion was 69.9% and the CO₂ production was 63 Kg per 100M Kg of DEG converted. While at 220°C, the DEG conversion was 86.0% and the CO₂ production was 133 Kg per 100M Kg DEG converted. Reaction Temp. (°C) DEG Conversion (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) per 100M Kg DEG Converted Morpholine DGA 210 69.9 62.4 34.0 45. 63 220 86.0 77.1 18.9 140 133 230 94.1 84.5 9.2 340 349 240 96.4 80.8 7.4 1110 1117 Time On Stream Hrs. DEG Conversion (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) per 100M Kg DEG Converted Morpholine DGA 24 65.6 58.7 38.0 118 170 48 65.9 58.7 38.0 130 201 72 68.0 60.1 36.7 143 213 100 67.1 57.8 38.6 165 251 Example 2 Following the operation procedures of Example 1 and using the same nickel-based dual catalyst system of nickel-copper-chromium oxides (400cc, bottom of reactor) and nickel-on-alumina (150cc, top of reactor) diethylene glycol amination was conducted at the same feed rates and back pressure, but at an operating temperature of 215°C. Data and results from this four-day run are summarized in Table II. It may be noted that in this experiment the average DEG conversion was ca.66.7%, while the CO₂ production was an average 209 Kg per 100M Kg of DEG converted. Example 3 Following the operating procedures of Example 1 and using the same nickel-based dual catalyst system of nickel-copper-chromium oxides (400cc, bottom of the reactor) and nickel-on-alumina (150cc, top of reactor), diethylene glycol amination was conducted at the same DEG and ammonia feed rate, but at a significantly higher hydrogen feed rate of 90 liters/hr. Again, the operation temperature and pressure were 215° and 15.27C MPa (2200 psi), respectively. Data and results from this four-day run are summarized in Table III. It may be noted that in this experiment, the average DEG conversion is ca. 77%, but the CO₂ production is now only 34 Kg per 100M Kg of DEG converted. Time On Stream (Hrs) DEG Conversion (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) per 100M Kg DEG Converted Morpholine DGA 24 78.1 73.7 18.3 25 28 48 78.0 77.8 15.9 40 48 72 75.6 72.6 17.9 20 26 100 76.4 76.0 15.3 23 32 Comparative Example A Following the operating procedures of Example 1, the 550cc plug flow reactor was filled with the nickel-copper-chromium oxide catalyst alone and diethylene glycol amination was conducted at feed rates of 0.54 Kg/h DEG, 1.09 Kg/h of ammonia and 35 liters/h of hydrogen. Again, the operating temperature and pressure were 220°C and 15.27 MPa (2200 psi), respectively. Analysis of the liquid and gas products shows: DEG Conversion 82% Yield of Morpholine 65.3% Yield of DGA 30.3% Effluent Conc. CO₂ 689 ppm CO₂ per 100M Kg DEG Converted 499 Kg Example 4 Following the operating procedures of Example 1, the same nickel-based dual catalyst system was employed but in different proportions. In this case the reactor was charged with 475cc of the nickel-copper-chromium oxides and with 75cc of the nckel-on-alumina at the top of the reactor. Two hydrogen flow rates were employed (35 and 90 liters per hour) and the operating temperature ranged from 210-230°C. The results are summarized in Table IV. It may be noted that at 90 liters/hr H₂, the CO₂ production was only 20-28 Kg/100M Kg DEG conv., when the operating temperature was in the range 210-220°C. Reaction Temp. (°C) H₂ Feed Rate (l/hr) DEG Conv. (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) per 100M Kg DEG Converted Morpholine DGA 210 35 79.7 63.6 31.1 130 168 215 35 88.6 73.1 21.1 230 265 220 35 93.1 79.1 14.9 370 407 230 35 98.3 88.2 5.2 940 987 210 90 79.6 71.7 17.0 19 24 215 90 91.0 77.5 6.7 19 20 220 90 95.8 78.0 4.1 30 28 Examples 5-7 Following the operating procedures of Example 1, different nickel-based dual catalyst systems were employed over a range of operating hydrogen feed rates (35-90 liters/hr) and temperatures (210-240°C). In each case 400cc of the nickel-copper-chromium oxide catalyst was employed in combination with 150cc of a supported nickel catalyst (at the top of the reactor). The second catalyst in each of these examples was as follows: Example 5 - A 41% Ni-On-Alumina, 50% reduced nickel, as spheres Example 6 - A 50%/Ni-On-Alumina, 50% reduced nickel, as spheres Example 7 - A 50% Ni on mixed oxide support, 45% reduced nickel, as tablets The results of these runs are summarized in Tables V to VII. All three catalyst combinations demonstrate substantial CO₂ suppression. Where The H₂ feed rate is 90 liters/h, the CO₂ production is lowered into the range of 12-41 Kg/100M Kg DEG converted. Reaction Temp. (°C) H₂ Feed Rate (l/hr) DEG Conv. (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) Per 100M Kg DEG Converted Morpholine DGA 210 35 67.6 63.3 33.3 94 140 220 35 82.5 75.7 20.7 270 321 230 35 93.4 84.2 10.0 780 758 240 35 96.6 84.4 4.9 2675 2595 220 90 88.1 73.3 11.6 40 41 220 90 89.2 73.2 10.0 30 27 Reaction Temp. (°C) H₂ Feed Rate (l/hr) DEG Conv. (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) Per 100M Kg DEG Converted Morpholine DGA 210 35 72.7 59.0 36.4 130 185 215 35 83.0 69.2 25.9 190 240 220 35 87.6 73.7 21.1 280 295 230 35 96.4 84.4 8.7 920 944 220 90 90.5 76.2 8.7 20 12 220 90 90.0 75.5 9.9 30 33 Reaction Temp. (°C) H₂ Feed Rate (l/hr) DEG Conv. (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) Per 100M Kg DEG Converted Morpholine DGA 210 35 71.7 58.4 36.6 103 150 215 35 81.8 67.9 26.8 184 240 220 35 88.7 76.7 18.4 300 356 230 35 96.6 85.7 7.7 830 847 220 90 91.4 75.3 5.9 26 30 220 90 90.3 76.3 7.1 22 27 Comparative Example B Following the operating procedures of Example 1, in this case the nickel-based dual catalyst system comprised 400cc of the nickel-copper-chromium oxide catalyst in combination with about 150cc of a nickel-copper-chromiuim-on-alumina catalyst containing about 47% nickel. The catalyst combination was evaluated for morpholine/DGA synthesis over a range of operating temperatures (210-250°C). The results are summarized in Table VIII. At about 80% DEG conversion, very little suppression of CO₂ was realized in comparison with Comparative Example A. Reaction Temp. (°C) H₂ Feed Rate (l/hr) DEG Conv. (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) Per 100M Kg DEG Converted Morpholine DGA 210 35 62.9 63.7 33.6 105 172 220 35 75.5 70.0 25.2 265 365 230 35 87.7 82.2 12.7 870 1052 240 35 90.5 77.6 10.8 2840 3224 250 35 88.0 68.2 12.5 4060 4790 Example 8 Following the operating procedures of Example 1, and using the same nickel-based dual catalyst system of nickel-copper-chromium oxides (400cc, bottom of reactor) and nickel-on-alumina (150cc, top of reactor), diethylene glycol amination was conducted over 500 hours using the same DEG, ammonia and hydrogen feed rates 0.54 Kg/h, 1.09 Kg/h, and 90 liters/h respectively). Operating temperature and pressure were 215°C and 15.27MPa (2200 psi), respectively. Data from this 500 hour run are summarized in Table IX. It may be noted that over the life of this experiment: 1) CO₂ production remains low (average 138 Kg/100M Kg DEG converted) and a factor of ca. 3.6 lower than in comparative Example A. 2) The DEG conversion level remains high. 3) There is no evidence of loss in morpholine plus DGA yields, or the formation of unwanted by-products, in comparison with the data for Ni-Cu-Cr oxide catalyst alone, in comparative Example A. Time On Stream (Hrs) DEG Conversion (%) Yield (%) Basis DEG Converted Effluent Conc. CO₂ (ppm) CO₂ (Kg) per 100M Kg DEG Converted Morpholine DGA 55 78.3 69.1 24.0 107 141 127 75.7 66.2 27.7 92 128 229 71.3 62.9 31.3 98 138 257 70.2 60.8 33.5 78 120 406 71.5 60.8 33.3 105 153 501 69.4 59.1 34.9 97 149

Claims: A process for simultaneously producing a morpholine and a 2-(2-aminoalkoxy)alkanol by reacting a dialkylene glycol with ammonia in the presence of added hydrogen over a nickel-copper-chromium oxide catalyst comprising 60 to 85 mole percent of nickel, 14 to 37 mole percent of copper, and 1 to 6 mole percent of chromium, characterized in that said catalyst is employed in combination with an oxide-supported nickel catalyst comprising 10 to 80% of nickel, on an oxide of an element of Group II, III or IV. A process according to Claim 1 characterized in that the dialkylene glycol has the formula: in which each R is independently hydrogen or alkyl. A process according to Claim 1 or 2 characterized in that the dialkylene glycol is diethylene glycol. A process according to any one of Claims 1 to 3 characterized in that the pressure is from 1.45 to 34.60 MPa. A process according to any one of Claims 1 to 4 characterized in that the temperature is from 150 to 300°C. A process according to any one of Claims 1 to 5 characterized in that the oxide support is alumina, silica, titania, zirconia, magnesia or a mixture thereof. A process according to any one of Claims 1 to 6 characterized in that the volume ratio of nickel-copper-chromium oxide catalyst to oxide-supported nickel catalyst is from 1:1 to 10:1

Inventors: KNIFTON JOHN FREDERICK, KNIFTON, JOHN FREDERICK
Applicants: HUNTSMAN CORP, HUNTSMAN CORPORATION
Application year: 1991
Main classification: C07D295
IPC codes: C07C213, C07D295, B01J23, C07B61, B01J32, C07C217