AMINES VIA THE AMINATION OF OLEFINS USING SELECT ZEOLITES

Abstract: This invention relates to an improvement in the vapor phase catalytic production of an amine by the reaction of a mixture comprising ethylene and ammonia. The improve­ ment which provides for high selectivity to the amine re­ sides in the use of an acidic erionite or clinoptilolite or mixture thereof as the catalyst.

Description: AMINES VIA THE AMINATION OF OLEFINS USING SELECT ZEOLITES TECHNICAL FIELD This invention relates to a process for producing amines by the reaction of ammonia or ammonia type compound with an olefin. BACKGROUND OF THE PRIOR ART The earliest work relating to the manufacture of amines by the amination of olefins particularly ethylamines by the amination of ethylene, appears to have been done by Teter et al as noted in U.S. Patents 2,623,061; 2,479,879; 2,417,892; 2,381,470; 2,658,041; 2,381,709; 2,392,107 and 2,398,899. These patents show that ammonia can be made to react with olefins, e.g. ethylene to produce amines. As noted by others through improvements in the process, substantial quantities of polyamines and polyolefins were produced by the Teter et al catalyst which is a metal supported on a spinel type support, silica and diatomaceous earth and the like. Olin et al in U.S. Patents 2,422,631 and 2,422,632, discloses a process for producing amines and amides by the reaction of a monounsaturated olefin, carbon monoxide and an amine or ammonia. The catalyst used is a combination of a dehydrating and a hydrogenation catalyst, e.g. nickel and activated alumina, copper and silica gel, etc. Whitman, U.S. 2,501,556 discloses a liquid phase reaction of ammonia and ethylene in the presence of an alkali metal catalyst to form ethylamine. McClain, U.S. 3,412,158 discloses a gas phase process for producing primary alkyl amines from low molecular weight olefins and ammonia by carrying out the gas phase process in the presence of a noble metal containing catalyst at temperatures of from 90-1750C, at pressures of from atmospheric to 2;000 psig. It is also known that alumino-silicates and particularly zeolites can be used for effecting amination of olefins at temperatures of 200-5000C, pressures from 300-6,000 psig. High yields and selectivity are reported. SUMMARY OF THE INVENTION This invention relates to an improved process for the preparation of ethylamines by the vapor phase catalytic reaction of ethylene'and ammonia. In the basic process ethylene is reacted at a temperature and pressure sufficient to effect formation of the amine, but controlled to prevent polymer formation. The improvement generally resides in the use of (a) a temperature from 300-4000C, (b) a pressure of from 300-2,000 psig and (c) an acidic alumino-silicate selectedfrom the group consisting of erionite, clinoptilolite and mixtures. There are several advantages either singly or combination associated with the invention as compared to many prior art processes. These advantages include: an ability to produce ethylamines in high selectivity without producing substantial by-products (greater than 8%), e.g. polymers in the form of polyolefins or hydrocarbons, e.g., linear, branched, or cyclic. The production of polymers has been a serious problem with many of the prior art processes; an ability to use a gas phase reaction which permits high production rate in producing amines; an ability to reduce the amount of by-product in the form of by-product nitrogen compounds e.g. nitriles as compared to prior art processes; an ability to obtain good to high conversion of ethylene to amine by virtue of the use of the particular catalyst and conditions employed and good catalyst life; and an ability to obtain a low aging rate with the particular catalysts. DESCRIPTION OF THE PREFERRED EMBODIMENT In the amination process ethylene is reacted with ammonia to produce the amine. Higher molecular weight olefins, e.g. propylene and butylene are more difficult to aminate with these catalysts and have extremely lower conversions. Presumably this is due to the small pore size of the catalyst and the large size of the higher amine molecules. Ammonia type reactants, e.g. primary and secondary amines also result in low conversion, presumably for the same reasons as the higher olefins. In the process, ammonia is reacted with ethylene at temperatures broadly from about 300-400 c. Lower temperatures result in lower conversion and higher temperatures result in lower selectivity which generally appears in the form of a nitrile or hydrocarbon. Pressures suited for practicing the invention are from about 300-2,000 psig with preferred pressures of from about 600-1100 psig. Generally, pressures lower than about 600 psig result in poor conversion of ethylene to amine. On the other hand, as the pressure is increased above about 1500 psig conversion is increased only slightly. In order to minimize the recovery problems associated with separating the amine from the reactants and other by-products, higher conversions can be waived and pressures of from about 600-1100 psig used as this permits extremely high selectivities, e.g. greater than 95%. Another important variable in the gas phase amination of the ethylene is the mole ratio of ammonia to ethylene in the feed. Generally, the mole ratio can be from about 0.2-20 moles ammonia per mole of ethylene with preferred ranges being from about 1-10 to 1 ammonia to ethylene. Mole ratios higher than about 10:1 of course require greater energy expenditure to handle the larger quantities of gas that pass through the reactor, and there seems to be no significant advantage in terms of increased selectivity or conversion at these higher ratios of ammonia to ethylene. On the other hand, as the mole ratio of ammonia to ethylene falls below about 0.2, there is a loss of selectivity to the amine. The gas hourly space velocity (GHSV), which has units of volume of gas per volume of catalyst in unit time i.e. (cc gas at STP)/(cc catalyst hours 1), can be from about 500-5,000 with a preferred range being from about 750-2,000. As the space velocity is increased toward the upper end of the range, conversion generally falls dramatically, particularly above about 3,000. On the other hand, as the space velocity approaches the lower level of 500, selectivity decreases and by-products form in greater concentration. One of the important factors in achieving the results of high selectivity to amines without the concomitant production of substantial amounts of. by products in the form of polymer, e.g. polyethylene; hydrocarbon or nitrogen compound as encountered in the prior art processes including those using zeolites is in the use of a highly acidic alumino-silicate selected from the group consisting of erionite, clinoptilolite and mixtures thereof. These zeolites are highly selective for the amination of ethylene and produce unique results. For example chabazite, which is a natural zeolite, gives lower conversion and selectivity even when used in combination with these zeolites. Thus, when using these catalysts at least about 80% by weight and preferably all of the catalyst is erionite, clinoptilolite or mixtures. It is believed the high acidity and narrow pore size of these alumino-silicates plays an important role in the catalyst activity and selectivity. Erionite and clinoptilolite are generally naturally occurring. Various ions can be incorporated into the zeolite by conventional techniques to provide acidity. Trivalent ions, and particularly the rare earth metals, i.e. lanthanum, neodymium, praseodymium, are well suited for preparing exchanged zeolites. Other cations which may be used in place of the original metal cations of the erionite or clinoptilolite include hydrogen, barium, beryllium, calcium, cerium, magnesium, potassium, silver and zinc. However, sodium and potassium tend to reduce activity presumably due to the lowering of the acidity of the catalyst. The crystalline alumino-silicate of the present invention may be employed alone or in combination with various binder or matrix materials (organic or inorganic materials, resins, clays, gels or the like). The physical form of the catalyst may be adapted to use in any conventional catalytic system (e.g. slurry or fluidized bed systems, beads, pellets or the like for use in fixed or moving bed catalysts). As is known, the hydrogen form of the zeolite can be prepared from the ammonium form and for purposes herein is referred to as the hydrogen form. The preferred metal ions for the exchanged zeolites are lanthanum and hydrogen as these provide good yields, good selectivity and good catalyst life. The following examples are provided to illustrate preferred embodiments of the invention and are not intended to restrict the scope thereof. EXAMPLE 1 A series of amination reactions 1-36 and 43-63 were carried out using a reactor consisting of a stainless steel tubing 9 inches long of 3/4" outside diameter and 5/16" inside diameter. The stainless steel reactor was mounted inside a close fitting block of Inconel metal which was instrumented for temperature control. A thermowell extending axially through the reactor was used to measure reactor temperature. The catalyst volume for the reactor was approximately 6 cubic centimeters and the catalyst was held in place by a quartz wool plug. The catalysts were sieved to pass through a 12 U.S. standard sieve but retained on an 18 mesh sieve. In the runs the experimental catalysts used were prepared from a 50-50 (as sold commercially by Anaconda Corp.) mixture of chabazite and erionite and from erionite and clinoptilolite separately, and SK 500. Such catalysts were prepared in the H form by conventional exchange of the naturally occuring zeolite followed by forming into pellets and heat treating. Comparisons were made against Linde SK-500 zeolite (REY.- a rare earth exchanged zeolite). A typical example of such catalyst preparation is as-follows: A 300 g sample of clinoptilolite was ammonium exchanged, then mixed with water to form an extrudable mix. This mixture then was thoroughly blended to assure homogeneity. After blending, the product was extruded into 1/8 inch pellets and dried. The dried product was heated at 8000F for 2 hours then crushed and sieved. Table 1 represents results for various catalysts including natural zeolites and reactor conditions. Table 2 is an average summary of work carried out in the manner of Table 1. MEA and DEA represent mono and di ethyl amine respectively. TABLE 1 AMINATION OF ETHYLENE NH3/Etthylene % Selectivity Run Olefin Catalyst T. C Psig CHSV Mole Ratio %Conv. Mono Amines Diamine Other 1 Ethylene H Chabazite 335 765 2000 4.1 1.9 100 Erionite'50 2 " " 350 765 2000 4.1 4.7 100 3 " " 368 765 2000 4.1 7.0 100 4 " " 370 765 2000 4.1 7.22 99 1 5 " " 385 765 2000 4.1 7.0 98 2 6 " " 340 750 2000 4.0 4.12 100 7 " " 360 750 2000 4.0 9.8 80.5 8 " " 370 750 2000 3.7 10.6 93 6 1 9 " " 370 750 2000 4.0 11.1 94 6 10 " " 380 750 2000 3.6 12.3 91 7.7 1.3 11 " Hchabazite-eriónite 320 750 2000 4.2 1.9 100 - 1.3 macroporous 12 " " 350 750 2000 4.0 5.3 100 13 " " 370 750 2000 4.2 10.5 95 5 14 " " 380 750 2000 4.3 11.3 94.4 5.6 15 " " 390 750 2000 4.4 12.6 82 4.1 13.9 In Runs 1-36 correction factors for Gc calibration have not been applied. When appliaed, % conversions will decrese about 15% from that statade. In Runs 43-63 a correction factor of 0.6 for MEA and 0.7 for C2H4 was introduced. TABLE 1 (CONTINUED) AMINATION OF ETHYLENE NH3/Etthylene % Selectivity Run Olefin Catalyst T. C Psig CHSV Mole Ratio %Conv. Mono Amines Diamine Other 16 Ethylene Clinoptilolite 340 750 2000 4.5 4.4 100 - 17 " " 340 750 2000 4.9 6.6 100 - 18 " " 360 750 2000 4.6 11.4 100 - 19 " " 370 750 2000 4.4 13.7 93.1 6.9 20 " " 370 750 2000 4.6 14.9 91.4 8.6 21 " " 380 750 2000 4.4 14.8 91.9 8.1 22 " " 380 750 2000 4.7 14.4 92 8 23 " " 390 750 2000 4.4 15.7 91 9 24 " " 400 750 2000 4.7 18 90.2 9.8 25 " SK-500 350 750 2000 4.6 3.9 100 - 26 " " 360 750 2000 4.3 7.5 100 - 27 " " 370 750 2000 4.3 9.4 96 4 28 " " 380 750 2000 4.2 12.1 92.6 5.4 29 " " 390 750 2000 4.0 12.8 81.9 4.5 13.6 30 " " 400 750 2000 3.8 13 69 2.0 28.9 31 " " 320 750 2000 4.0 - 32 " " 335 750 2000 4.0 2.5 100 33 " " 335 750 2000 3.8 2.9 100 34 " " 355 750 2000 4.3 3.4 100 35 " " 360 750 2000 3.8 8.8 97 3.0 36 " " 370 750 2000 4.1 12.3 90 7.3 2.7 TABLE 1 (CONTINUED) AMINATION OF ETHYLENE NH3/Etthylene % Selectivity Run Olefin Catalyst T. C Psig CHSV Mole Ratio %Conv. Mono Amines Diamine Other 43 " H Erionite 360 750 2000 3.4 9.3 88.5 10.7 0.8 44 " " 375 750 2000 8.0 15.5 88.4 10.5 1.1 45 " " 380 750 2000 3.5 12.3 84.7 13.8 1.5 46 " " 380 750 2000 5.2 9.9 88.5 8.8 2.7 47 " " 380 750 2000 4.1 13.5 83.3 12.3 2.6 48 " " 380 750 2000 4.7 12.9 87.8 10.0 2.2 49 " " 380 750 2000 5.5 13.0 88.4 8.7 2.9 50 " " 380 750 2000 5.6 14.4 87 8.5 4.5 51 " " 390 750 2000 5.8 15.1 86.2 8.4 5.0 52 " " 390 750 2000 5.8 16.3 84.3 8.6 5.6 53 " " 400 750 2000 5.7 17.5 77.7 7.7 14.6 54 " " 400 750 2000 5.8 17.9 78.6 7.9 13.2 55 " " 320 750 2000 3.8 1.6 90.8 3.7 5.5 56 " " 320 750 2000 4.3 2.8 95.4 4.5 57 " " 340 750 2000 4.7 3.5 97.2 2.7 58 " " 360 750 2000 4.5 7.4 92.4 6.7 0.8 59 " " 360 750 2000 3.0 8.7 88.6 10.5 1.0 60 " " 370 750 2000 2.7 10.2 86.2 12.5 1.2 61 " " 380 750 2000 3.2 13.4 85.4 11.7 1.7 62 " 380 750 2000 4.0 15.2 85.7 12.5 2.3 63 " " 400 750 2000 3.9 16.5 84.2 13.1 2.5 Table 2 Comparison of Ethylene Conversion and Amine Selectivity as a Function of temperature Temp. SK500* H-clinoptilolite H-erionite A B A B A B 320 -- -- 2.2 100 2.9 100 340 1.5 100 5.6 100 5.26 100 350 3.3 100 360 5.3 100 9.7 100 8.76 99.2 370 8.0 100 11.7 100 12.52 98.7 380 10.3 98 12.6 100 15.2 97.3 390 10.8 86.4 14.6 100 400 11.0 71 15.3 99.6 16.9 94 = % C2H4 conversion was corrected by introducing correction factors of 0.7 and 0.6 for C2H4 and MEA respectively. A = % ethylene conversion. B = selectivity to ethylamines. These summarizing data show that the H-clinoptilolite and H erionite consistently gave better selectivity and better conversion than SK-500 at a given temperature and pressure, mole ratio, etc. The data in Table 1 show better conversion for these catalysts than with the chabazite mixtures even when "uncorrected" in runs 1-36. From the data in the tables it is clear that the erionite and clinoptilolite catalysts are extremely effective for the amination of ethylene and they were more effective than the standard Linde SK-500 zeolite (a rare earth exchanged Y zeolite), and chabazite mixtures. Conversions were significantly higher particularly with the H-clinoptilolite and H-erionite catalyst at temperatures from about 370-4000C. In those cases where conversions were forced with SK-500, the corresponding selectivity to the desired amine products was lower than where higher conversions were achieved using clinoptilotite and erionite, note runs 19-30 and Table 2. Another interesting point about H clinoptilolite and H erionite is that only a small fraction of the product was non-amine even at high conversions whereas higher by-product levels were experienced with SK-500. Runs 29, 30 and 61-63 show this point. The higher catalytic activity of H-clinoptilolite and erionite as noted above was attributed to the higher acidity of the catalyst. To confirm this belief, acidity distribution was measured. A thermal gravimetric analysis technique with ammonia as an adsorbate was used. The acidity measurement being performed by activating about 20-40 mg of catalyst at temperatures up to 4000C in helium, after which the catalyst was cooled at 250C. The uptake of ammonia by the catalysts was very fast and the catalyst surface saturated within 5 minutes. Helium was then used to desorb the physically adsorbed ammonia at 250C followed by heating the catalyst to 100, 200, 300, and 4000C respectively to desorb physically adsorbed ammonia. The temperature was taken up after there is no change in the rate of desorption (as noted by decreasing weight). The amount of irreversibly adsorbed ammonia at each temperature was taken as a count of acid sites. The amount of irreversibly adsorbed ammonia at 25 and 1000C was considered as a count of total acidity (weak plus strong acid sites) and that at 200 and 3000C as strong acidic sites. The strong acidic sites were considered as the number of surface active sites for ethylene amination. Table 3 shows a comparison of acidic site distribution over SK-500, H-clinotilolite, and H-erionite. The acidity of these materials decreases in the order H-erionite, H-clinoptilolite and SK-500. The same trend was observed for the amination activity. The enhanced acidity of H-erionite and H-clinoptilolite over SK-500 also would explain the superior activity of the catalysts, while the better selectivity may be related to the pore shape structure. Table III The Number of Acid Site Distribution (mmoles of ammonia/g. of dry catalyst) Tempos Catalyst 25 100 200 300 SK-500 3.3 1.8 0.9 0.4 H-clinoptilolite 3.6 2.1 1.2 0.8 H-erionite 3.9 1.9 1.5 1.0 A comparison of H-erionite with SK-500 in ethylene amination was made using an ammonia to ethylene ratio of 4:1, a space velocity of 1000 hr. 1, and a temperature of 365 c. With SK-500, at the end of 20 days operation, propylene was observed and conversion had dropped from about 11 to about 8% by weight. On the other hand, after 42 days service the H-erionite catalyst was yielding 11% conversion. The calculated deactivation rate for SK-500 was 0.234%/davy and for H-erionite it was less than 0.07%/day. Although not intending to be bound by theory, another explanation for the enhanced conversion, selectivity and catalyst life at high temperatures is as follows: The sorption cavities in erionite constitutes a three dimensional net work of pores. Each cavity has a length of 15.1A and a free cross-sectional diameter of 6.3 to 6.6A. Reactants and products can enter or leave the cavity through six elliptical openings each has a minimum and maximum diameter of 3.5 and 5.2A respectively. These pores are large enough to allow uptake and egress of C2H4 (and other linear olefins ) but too small to allow the formation of branched or cyclic hydrocarbons. The same analogy can be made for clinoptilolite. The free cross-section of these materials is different from A, X, or Y zeolites. The latter have spherical type cages with diameters of about 11-13A. This would allow the formation of large molecules (branched and cyclic) localized or strongly chemisorbed organic polymer of low mobility inside the pores which would result in blocking or obliteration of active sites. This of course would permit the formation of unsaturated and higher molecular weight organics and reduce conversion. The use of zeolites with a smaller pore system (erionite or clinoptilolite) decreases the chance of ethylene polymerization, isomerization, and cyclodehydrogenation and eventually "coke" formation. This results in a much longer catalyst life compared to those of the large pore zeolites.

Claims: What is Claimed is: 1. In a vapor phase catalytic amination process for the production of amines from a reaction mixture comprising ethylene and a nitrogen compound consisting of ammonia at a temperature and pressure sufficient for effecting formation of said amine the improvement which comprises: empldying as a catalyst for said process an alumino-silicate selected from the group of zeolites consisting of erionite, clinoptilolite and mixtures. 2. The process of Claim 1 wherein said aluminosilicate is acidic. 3. The process of Claim 2 wherein said alumino silicate is rare earth or hydrogen ion exchanged. 4. The process of Claim 3 wherein the pressure in said amination is from 600-1100 psig, and the gas hourly space velocity is from 500-5,000. 5. The process of Claim 4 wherein the temperature in said amination is from 300-400 C. 6. The process of Claim 5 wherein the mole feed ratio of ammonia to ethylene is from about 1-10:1. 7. A method for making amines which comprises contacting ethylene and ammonia in the vapor phase with a catalyst and an acidic alumino-silicate selected from the group consisting of erionite and clinoptilolite or mixtures thereof under amination conditions which include a temperature in the range of about 300-400"C, a pressure in the range of about 600-1100 psig, a mole ratio of ammonia to olefin of about 1-10:1 and a gas hourly space velocity of about 500-5000. 8. The process of Claim 7 wherein said acidity is provided by trivalent rare earth metal or hydrogen ions.

Inventors: AMBS, WILLIAM J., DEEBA, MICHEL
Applicants: AIR PRODUCTS AND CHEMICALS, INC.
Application year: 1982
Main classification: C07C85
IPC codes: C07B61, B01J21, C07C209, B01J29, C07C67