Nitrogen-selective zeolitic adsorbent for use in air separation process

Abstract: In using calcium-exchanged forms of zeolite X as selective adsorbents for nitrogen in PSA air separation process, it has been discovered that, particularly under certain temperature and pressure conditions, superior performance is not, as is generally believed, obtained when the calcium content is at a maximum, but rather when the degree of calcium exchange is in the range of 60 to 89 equivalent percent and only when the framework Si/Al 2 ratio of the zeolite is within the range of 2.0 to 2.4

Description: The present invention relates in general to use of a novel zeolitic adsorbent in air separation processes to selectively adsorb nitrogen and, more particularly, to the use in such processes of a nitrogen-selective adsorbent containing zeolite X having a framework Si/Al 2 ratio of 2.0 to 2.4 and having a specific cation population. BACKGROUND The separation of air into its two principal constituents, nitrogen and oxygen, is an important commercial operation which produces several hundred billion cubic feet of each material every year. Where large quantities of either constituent are required, as, for example, oxygen in the manufacture of steel, the large capital costs of cryogenic systems can be justified, and cryogenic procedures are generally employed. For operations with smaller requirements, oxygen and nitrogen can also be produced by pressure-swing adsorption (PSA) processes. In PSA processes, compressed air is pumped through a fixed bed of an adsorbent exhibiting an adsorptive preference for one of the main constituents whereby an effluent product stream enhanced in the non-adsorbed (or lesser adsorbed) constituent is . obtained. Compared to the cryogenic processes, PSA air separation processes require relatively simple equipment and are relatively easy to maintain. PSA processes, however, have lower product recovery and higher energy consumption than the cryogenic processes. For these reasons, improvements in the adsorption processes remain an important goal. One principal means of improvement is the discovery and development of better adsorbents. The use of crystalline zeolitic molecular sieves as selective adsorbents for nitrogen, particularly from air, is well known in the art. The general class of zeolites having pore diameters of at least 4.6 Angstroms was proposed in US-A-3140931 for this service. The use of the particular zeolite species, zeolite X, containing as cations at least one member of the group consisting of strontium, barium or nickel was proposed for this separation in US-A-3140932. The relative merits of the various alkali metal cation forms of zeolites, including zeolite X, were discussed in US-A-3140933. In US-A-4557736, a binary ion-exchanged form of zeolite X was taught as a preferred adsorbent for the adsorption of nitrogen from air. In US-A-4481018, a set of activation conditions which substantially avoids both frame work and cation hydrolysis in polyvalent cation forms of faujasite is disclosed. These compositions, particularly in the Mg 2+ , Ca 2+ , Sr 2+ , and/or Ba 2+ cation forms, are alleged to be superior adsorbents for the separation of nitrogen from air. Based on selectivity values for N 2 /O 2 obtained from gas chromatographic studies, this '018 patent teaches that the higher the degree of Ca 2+ exchange the greater the selectivity and capacity of the faujasite-type adsorbent for the separation of nitrogen from air. The minimum calcium content disclosed is 50% and the preferred adsorbents contain greater than 80 equivalent percent calcium cations. In sum, calcium, strontium and lithium cations are viewed by the prior art as desirable constituents of zeolitic adsorbents for use in nitrogen separation. Other cations such as sodium are viewed as less desirable. EP-A-0685429 is a document falling within the state of the art in certain contracting states of the European Patent Convention in accordance with the provisions of Article 54(3) and (4) EPC. It relates to a crystalline metallosilicate composition comprising an EMT structure with a Si/X ratio of less than 2.0 and a micropore volume in the sodium and/or potassium form of at least 0.20 cm 3 /g, wherein X is selected from the group consisting of aluminium, boron and gallium. According to a preferred embodiment, the EMT structure is in an intergrowth with an FAU crystalline structure. EP-A-0685429 also provides a process for making the metallosilicate compositions, and processes for adsorptively separating gases using the compositions. EP-A-0685429 explains that the EMT structure exhibits hexagonal symmetry, while the FAU structure exhibits cubic symmetry. EP-A-0743281 is also a document falling within the state of the art in certain contracting states of the European Patent Convention in accordance with the provisions of Article 54(3) and (4) EPC. It relates a process for the oxygen enrichment of air by vacuum swing adsorption, pressure swing adsorption or a combination thereof, which comprises providing a packing at the air inlet side of the adsorber comprising Na-Ca zeolite X with an SiO 2 /A1 2 O 3 ratio of 2.0 to 2.5 and CaO/A1 2 O 3 ratio of 0.4 to 0.75, the ratio being dependent upon the air inlet temperature, and a packing at the air outlet side of the adsorber comprising Na-Ca zeolite A with a CaO/A1 2 O 3 ratio of 0.5 to 1.0 or Na-Ca zeolite X with CaO/A1 2 O 3 ratio of 0.4 to 1.0, above the CaO/A1 2 O 3 ratio of the Na-Ca zeolite X at the inlet side. EP-A-0486384 describes an industrial adsorbent for the non-cryogenic separation of gases from air, comprising from 70 to 95% by weight zeolites, and, correspondingly, from 30 to 5% by weight of a clay binder. The zeolites are mixtures of X and A zeolites having an X crystallinity greater than or equal to 95% and an A crystallinity less than or equal to 5%, a toluene standard adsorption of 23 ± 1% and an X-ray spectrum characteristic of a practically pure faujasite, and with the Si/Al ratio of the crystalline component being 1 ± 0.03. and the adsorbent has a 2Ca/Al ratio between 80 and 99%, a nitrogen adsorption between 16 and 23.5litre/kg and a ratio of the nitrogen to the oxygen adsorption capacities under 1 bar between 3.5 and 4.5. BRIEF DESCRIPTION OF THE DRAWINGS Fig 1 plots nitrogen residual loadings of CaNaX2.0 (i.e. X zeolite having a silica/alumina ratio of 2:1 and Ca 2+ and Na 1+ cations) after desorption to 10.7 kPa (1.55 psia) as a function of calcium exchange level at 40°C, 20°C and 0°C, respectively. Fig. 2 plots nitrogen delta loading of CaNaX2.0 between 14.7 and 1.55 psia as a function of calcium exchange level at 40°C, 20°C and 0°C, respectively. Fig. 3 plots nitrogen operational selectivity of CaNaX2.0 as a function of calcium exchange level at 40°C, 20°C and 0°C, respectively. Figs. 4, 5, and 6 plot nitrogen residual loading, delta loading, and operational selectivity of CaNaX2.3 as a function of calcium exchange level at 40°C, 20°C and 0°C, respectively. Figs. 7, 8, and 9 plot nitrogen residual loading, delta loading, and operational selectivity of CaNaX2.5 as a function of calcium exchange level at 40°C, 20°C and 0°, respectively. Fig. 10 gives desorption rate of CaX2.0 (97% Ca) at 22°C. Fig. 11 gives desorption rate of CaNaX2.0 (75% Ca) at 22°C. Fig. 12 gives desorption rate of CaX2.3 (97% Ca) at 22°C. Fig.13 gives desorption rate of CaNaX2.3 (77% Ca) at 22°C. Fig. 14 gives desorption rate of CaX2.5 (97% Ca) at 22°C. Fig. 15 gives desorption rate of CaNaX2.5 (77% Ca) at 22°C. It has now surprisingly been found that zeolite X, particularly those forms having a SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.4 and containing from 60 to 80 equivalent percent Ca ++ cations, from 10 to 40 equivalent percent Na + cations and from zero to 10 percent K + cations, the total cation equivalency contributed by Ca ++ , Na + and K + being at least 90 percent is significantly more effective as an adsorbent for the separation of air in a pressure swing adsorption process in the temperature range of 50 to -20°C at pressures in the range of 5 to 506.5 kPa (0.05 to 5.0 atmospheres) than is the same zeolite X which has been calcium exchanged to a greater or lesser extent. Such zeolites that contain k + cations are claimed herein as novel absorbents. Accordingly the present invention resides in a cyclic process for separating nitrogen from a mixture thereof with oxygen which comprises the steps of: (a) providing an adsorption bed containing an adsorbent wherein the absorbents consists of a zeolite X having a framework SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.4 and containing from 60 to 80 equivalent percent Ca ++ cations, from 10 to 40 equivalent percent Na + cations and from zero to 10 percent K + cations, the total cation equivalency contributed by Ca ++ , Na + and K + being at least 90 percent; (b) passing said mixture of nitrogen and oxygen into said adsorption bed at a temperature of from -20 to 50°C until an internal bed pressure rises to the range of 13.8 to 506.8 kPa (2 to 73.5 psia) and nitrogen is selectively adsorbed on said adsorbent: (c) discharging unadsorbed oxygen as a product from the adsorption bed substantially at the adsorption pressure; and (d) decreasing the bed pressure to a final desorption pressure within the range of 101.4 to 0.7 kPa (14.7 to 0.1 psia) to desorb the adsorbed nitrogen and discharge desorbed nitrogen from the bed. In a particularly preferred embodiment of the process according to present invention the zeolite X adsorbent has a SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.35, its cation population comprising from 65 to 80 equivalent percent Ca ++ cations and from 20 to 35 equivalent percent Na + cations, said zeolite being substantially free from K + cations. It is well known that nitrogen has a quadrupole moment of 0.31 A 3 and for that reason interacts more strongly with zeolitic cations than does oxygen, which has a quadrupole moment of only about 0.1 A 3 Being more strongly adsorbed, nitrogen is more strongly adsorbed on zeolites from mixtures of nitrogen and oxygen in accordance with thermodynamic principles. This selectivity for nitrogen adsorption is the basis for the numerous air separation process utilizing fixed-bed pressure-swing adsorption-desorption cycles. The properties of the zeolite cations are the most important factors which bear on the selectivity and capacity for nitrogen adsorption. Lithium and calcium as zeolitic cations have been shown to exhibit particularly strong affinities for nitrogen. In the case of calcium-exchanged forms of zeolite X, the effect of increasing calcium content has been reported in US-A-4481018. Therein it is alleged that better selectivity and capacity is achieved when the calcium cation content exceeds about 80 equivalent percent. The improvement in nitrogen adsorption efficacy is ascribed to the fact that the calcium and other polyvalent metal cations of the zeolite X employed are predominantly in the dehydrated/dehydroxylated state. In view of these teachings, it is the general understanding by those skilled in the art that where a particular metal cation form of zeolite exhibits good adsorptive properties with respect to nitrogen, the higher the content of that particular metal cation the better the performance in air separation. It has now unexpectedly been found that in the case of calcium-exchanged forms of zeolite X, the peak performance in air separation under certain temperature and pressure conditions is not obtained when the calcium content is at a maximum, but rather when the degree of calcium exchange is in the range of 60 to 80 equivalent percent, especially in the range of 65 to 80 equivalent percent. It is even more surprising to find that the improvement caused by the reduced calcium exchange level results in an effective adsorbent only if the SiO 2 /Al 2 O 3 ratio of X zeolite is in the range of 2.0 to 2.4. While not wanting to be bound by any particular theory or theories, it is believed that too much reliance has heretofore been placed on the charge density of the calcium cation without due regard for other factors. At least with respect to calcium-exchanged forms of zeolite X, hereinafter designated CaNaX, the nitrogen selectivity and capacity are complex functions of cation composition and zeolite structure as well as the temperature and pressure conditions under which the adsorbent and the nitrogen containing gas are brought into contact. The nitrogen selectivities of CaNaX compositions reported in the literature are often measured with chromatographic techniques, with the nitrogen pressure over the adsorbent being quite low. Since the nitrogen selectivity of CaNaX is sensitive to pressure, the high selectivity values reported are not applicable to higher nitrogen pressures. The present invention is based at least in part upon the discovery that, depending upon the level of calcium exchange, the nitrogen selectivity of CaNaX can drop significantly as pressure increases. Furthermore, pressure used in the adsorption step of a practical commercial scale air separation process is substantially higher than the nitrogen pressure in a chromatographic measurement. Therefore, the selectivity as determined by chromatographic method has very little relevancy to the adsorption step in a commercial pressure swing adsorption process. In a PSA air-separation process, desorption is a required process step. For an efficient adsorbent, a maximum decrease of nitrogen loading over the shortest desorption time interval must be achieved, so that the adsorbent can be regenerated with minimal use of a vacuum pump or the oxygen product. In other words, in order to have an efficient desorption step in a PSA air separation process it is necessary for the adsorbent to have a low nitrogen affinity at the desorption or purge pressure. Since the nitrogen pressure in a chromatographic measurement is well within the desorption pressure of a PSA process, a high nitrogen selectivity observed chromatographically suggests that such an adsorbent will have poor desorption characteristics in a PSA process. Ideally, for PSA air separation, an adsorbent should exhibit a low nitrogen affinity at low pressures and a high nitrogen affinity at high pressures. In theory, and confirmed by actual experience, it is not possible to have such a nitrogen adsorbent. The next best thing is an adsorbent whose nitrogen selectivity does not decline steeply as the adsorbate pressure increases. In accordance with the present invention it has been found that for CaNaX adsorbents, the decrease in nitrogen affinity with increasing nitrogen pressure is, to a significant degree, dependent upon the level of calcium ion exchange. For highly calcium X, i.e., 90 equivalent percent or greater, the decrease in nitrogen affinity is steep. For CaNaX having a 60 to 80 % Ca ++ level, the affinity for nitrogen at very low pressures is not very high and it does not decrease rapidly when pressure increases. As a result, the operational nitrogen selectivity of moderately calcium-exchanged CaNaX can be higher than that of high CaX. More importantly, at the desorption pressure the nitrogen is easily desorbed from the moderately exchanged CaNaX, thus significantly facilitating the regeneration of the adsorbent. As a result the overall performance of the particular CaNaX compositions employed in this invention is significantly better than that of the more highly exchanged CaX. To evaluate the potential of a material as a PSA air separation adsorbent, the following three criteria should be considered: 1. Residual nitrogen loading which is the nitrogen loading at the desorption pressure. A good PSA air adsorbent should have low residual nitrogen loading. 2. The nitrogen delta loading which is the difference between the loading at adsorption pressure and the loading at the desorption pressure. A good PSA air adsorbent should have a high nitrogen delta loading. 3. The operational selectivity which is defined as the nitrogen delta loading divided by the oxygen delta loading. A good air separation adsorbent should have a high operational selectivity for nitrogen. The temperature at which the process is to be carried out is also an important factor in the performance of adsorbents in air separations. Industrial PSA air separation vessels are usually large and process cycle times are short relative to the time needed to heat up or cool down the massive amount of adsorbent involved. As a consequence, the process cycle is carried out under adiabatic or near adiabatic conditions. The heat of adsorption of nitrogen on CaNaX zeolites is significant. The heat released by adsorption is carried forward by the feed and product gas and accumulates to form a heat front. A portion of the heat front may leave the column with the product gas. The remaining portion of the front is pushed back into the column during the desorption stage of the process cycle. During the desorption, kinetic energy is consumed to free nitrogen from the adsorbent and thus reduces the temperature of nitrogen and the adsorbent. The heat of desorption creates a cold front in the bed, a portion of which leaves the bed along with the waste gases. The remaining portion of the cold front is pushed backward through the column by the feed gas during the next adsorption step. After many adsorption-desorption cycles a steady state will be reached. At the steady state, some portion of the bed can be significantly cooler than ambient. It is, therefore, imperative to utilize an adsorbent whose adsorptive properties are not unduly impaired by such temperature changes. The present invention is based in part upon the determination that the adsorptive properties of highly calcium exchanged forms of zeolite X are easily impaired by a drop in temperature but in the case of the moderately exchanged CaNaX are not so impaired. Even a moderate decrease of adsorption temperature can greatly increase the residual nitrogen loading and decrease the nitrogen operational selectivity of a highly calcium exchanged X zeolite. Our investigations also establish that adiabatic desorption will cause a greater temperature drop on high CaX than on CaNaX. In a PSA air separation process, the productivity of adsorbent is determined not only by the nitrogen delta loading and the nitrogen operational selectivity but also by length of cycle time. An adsorbent which can function in a shorter cycle time will have a higher production rate. The cycle time is determined by how rapidly the adsorbent can be regenerated and made ready for the next adsorption step. It has been found that nitrogen desorbs much faster from a moderately exchanged CaNaX than from a highly exchanged CaX. In sum, after taking PSA air separation conditions into consideration, it has been found that moderately calcium exchanged CaNaX is a superior adsorbent to highly exchanged CaX. The present invention is illustrated and exemplified by the data shown in tabular form in TABLES I through V and in the graphs of Figures 1 through 15 of the drawings. The following adsorbent compositions, the methods for their preparation and the testing procedures were utilized in obtaining the aforesaid data: Preparation of the Starting Zeolite X Compositions: Samples of Zeolite X having Si/Al 2 molar ratios of 2.0, 2.3 and 2.5, respectively, were prepared. The sample having a Si/Al 2 ratio of 2.0 was synthesized hydrothermally at 70°C in the mixed Na + - K + cation form, i.e., NaKX2.0, in accordance with the technique disclosed in British Patent 1,580,928, using sodium hydroxide, potassium hydroxide, sodium silicate, aluminum hydroxide and water as the reagents. As initially crystallized, the NaKX2.0 contained about 25 equivalent percent K + cations with the remainder being Na + cations. The K + cations were substantially all removed and replaced by Na + cations by a thorough ion exchange using an aqueous NaCl solution. Certain of the test procedures reported hereafter were performed on pure, i.e., unbonded, zeolite samples, and in others bonded agglomerates were utilized. In the latter case, the binding agent was an attapulgite-type clay available from the Floridin Company under the trademark Minugel. The agglomerates, in the form of beads and extruded pellets, were prepared by conventional methods well known in the art. To prepare partially calcium exchanged adsorbents, a batch exchange technique was used. The zeolite, either in powder or aggregate form, was immersed in a calcium chloride solution at 80 to 95°C with constant agitation. Typically this operation lasted 1 to 2 hours. The calcium exchange level was controlled by the quantity of zeolite and calcium chloride used. To prepare high calcium exchanged zeolite X powder, a technique of repeated batch exchange with great excess of calcium chloride was used. To prepare high calcium exchanged aggregates, a column exchange technique was used. Zeolite aggregates were placed in a heated column and preheated calcium chloride solution was passed through the column to displace and flush away the exchanged sodium or potassium ions. Further details of the ion-exchange procedures appear in the numbered Examples, below. Example 1. In this Example are reported the preparation, composition and adsorption properties of those CaNaX compositions in which the Si/Al 2 framework ratio is 2.0. These compositions are denominated CaNaX2.0. The CaNaX2.0 samples were prepared by batch ion-exchanging NaX2.0 clay-bonded agglomerates in the form of 8x12 beads. In general, 50 grams of starting NaX2.0 beads (dry weight) were added to 1 to 2 liters of aqueous 0.15M to 1M CaCl 2 solution adjusted to a pH of 9.0 using Ca(OH) 2 . In each instance the exact quantity and concentration of the CaCl 2 solution were selected in view of the targeted degree of Ca ++ ion-exchange to be achieved. Where necessary, multiple batch exchange procedures were used to obtain a product of the desired degree of ion-exchange. In each batch exchange the zeolite-containing beads were stirred in the CaCl 2 solution while the solution was heated from ambient room temperature up to 90°C and thereafter the stirring continued for one hour. The exchanged beads were recovered by filtration in a Buchner funnel and rinsed with 500 ml of hot water at a pH of 9.0 adjusted by the addition of Ca(OH) 2 . Thereafter the beads were stirred in 1 liter of water at 90°C and a Ca(OH) 2 -adjusted pH of 9.0 for 30 minutes, recovered by filtration and dried in air. In all, seven CaNaX2.0 samples, denominated hereinafter as 1a through 1g, respectively, were prepared. The particulars of the preparations and the chemical compositions of the products are set forth in Table I and Table II, respectively, below. All of the agglomerate beads contained 12 wt. % clay binder. Example 2. Six powder and two beaded samples of calcium-exchanged NaX having a Si/Al 2 molar ratio of 2.3 were prepared by the same general procedures described in Example 1. The principal difference in the procedures was the temperature of the ion-exchange medium which was 95°C in these preparations instead of the 90°C temperature used in Example 1. The details of the ion-exchange procedures and the chemical composition of the ion-exchanged products, denominated as samples 2a through 2h, are set forth below in Table I and Table II, respectively. Example 3. Using an as-synthesized sodium zeolite X having a Si/Al 2 molar ratio of 2.5, clay-bonded 8 x 12 beads were ion-exchanged with Ca ++ ions. Four samples, denominated 3a through 3d, respectively, were prepared. Samples 3a and 3b were ion exchanged using the batch technique of Examples 1 and 2, and samples 3c and 3d were ion-exchanged using the column technique wherein an aqueous CaCl 2 solution is passed through a heated column containing the zeolite-containing beads. Details of the ion-exchange procedures and the chemical compositions of the exchanged products are set forth in Table I and Table II, respectively. Example 4. The nitrogen and oxygen isotherms of activated samples 1a through 1g and the NaX2.0 starting material of Example 1 were determined at 40°C, 20°C, 0°C and -20°C using a Sartorius balance. The samples were activated in a glass tube in a system equipped with an oil diffusion pump and a liquid nitrogen trap by heating from ambient room temperature up to 510°C over the period of 10 hours and maintaining the final temperature for 6 hours. A pressure of 1.33 x 10 -6 kPa (1 x 10 -5 torr) was achieved at the end of the activation procedure. In the measurement of the nitrogen and oxygen isotherms the temperature of each test sample was controlled by placing the sample chamber in a constant temperature bath or a tube furnace, as appropriate. Between 0 to 506.7 kPa (zero psia to 73.5 psia), 13 data points were taken. The nitrogen loadings at exactly 10.7 to 101.4 Kpa (1.55 and 14.7 psia) were determined by intrapolation. The difference of the two values is the nitrogen delta loading. The oxygen loadings at 25.5 kPa (3.7 psia) were also determined by intrapolation. The nitrogen delta loading divided by the oxygen delta loading between 25.5 kPa (3.7 psia) and 0 kPa (zero psia) gives what is termed the operational selectivity. Values of residual loading, delta loading and operational selectivity are listed in Table III below, and plotted in Figures 1, 2 and 3 of the drawings. Example 5. Following the procedure described in Example 4, supra, the nitrogen residual loading, nitrogen delta loading and the nitrogen operation selectivity of NaX2.3 and CaNaX2.3 samples of 2a through 2h, respectively, of Example 2 were determined. The results are tabulated in Table IV. All of these samples are unbonded, i.e., they do not contain clay, zeolite powder. Figs. 4, 5 and 6 of the drawings disclose residual loadings and operational selectivity data as functions of calcium exchange levels and adsorption temperatures. Example 6. Following the procedure described in Example 4, supra, the nitrogen residual loading, nitrogen delta loading and the nitrogen operation selectivity of NaX2.5 and CaNaX2.5 samples 3a, 3b and 3c of Example 3 were determined. The results are tabulated in Table V. Figures 7, 8 and 9 of the drawings disclose residual loadings and operational selectivity data as a function of calcium exchange levels and adsorption temperatures. Example 7. To evaluate the desorption time needed for an adsorbent in a PSA cycle, the nitrogen desorption rate was measured with a Sartorius balance. The activated adsorbent was first brought into contact with nitrogen at a pressure of 101.3 kPa one atmosphere). After adsorption equilibrium was reached, the gas was rapidly evacuated by a vacuum pump. The pump down step was terminated when pressure reached 1.4 kPa (0.2 psia). It required about 10 seconds to reach that pressure. The adsorbent was then allowed to reach its equilibrium and the weight loss of the adsorbent was continuously monitored. The final pressure in the Sartorius balance is a function of adsorption capacities of the adsorbent. For CaNaX of various silica to alumina ratios and different calcium exchange levels, the final pressure is in the range of 1.72 to 2.62 kPa (0.25 to 0.38 psia). Since nitrogen has large heat of desorption, a rapid desorption under adiabatic conditions causes a drop in adsorbent temperature. Vacuum desorption in a Sartorius balance closely approximates an adiabatic process. It is, however, very difficult to measure the sample temperature in a Sartorius balance directly, and accordingly the temperature after desorption was estimated by a comparison of the residual loading with the nitrogen isotherms at 20°, 0° and -20°C, respectively. (a) The nitrogen desorption curve for sample 1g of Example 1, a highly calcium exchanged (97%) zeolite X having a Si/Al 2 molar ratio of 2.0, is shown in Fig. 10 of the drawings. To obtain the data, the vacuum-activated sample was first equilibrated in the Sartorius balance with nitrogen at 112.4 kPa (16.3 psia). The balance was then rapidly evacuated to 1.38 kPa (0.2 psia) and the sample allowed to reach equilibrium with a consequent rise in pressure to 2.62 kPa (0.38) psia). Also shown in Fig. 10 are the expected equilibrium nitrogen loadings at 2.62 kPa (0.38 psia) for the temperatures 20°C, 0°C and -20°C as determined by extrapolation from 10.3 to 2.62 kPa (1.5 to 0.38 psia). It appears from these data that the desorption in the Sartorius balance likely chilled the zeolite sample temperature to about 0°C. (b) Using essentially the same procedure as in part (a) above, the nitrogen desorption curve for Sample 1d of Example 1 containing 75 equivalent percent calcium cations was determined. These data are set forth in Fig. 11. The final nitrogen pressure in the balance was 1.72 kPa (0.25 psia) and the residual loading about 0.09 mmol/gram. From inspection of the expected equilibrium nitrogen loadings at 1.72 kPa (0.25 psia) (by extrapolation from 10.3 kPa (1.5 psia)) and 20°C, 0°C and -20°C also shown in Fig. 11, the sample appears to have been chilled during desorption to a temperature of about 10°C. (c) Using the sample procedure as in part (a) above, the nitrogen desorption curves for Sample 2h of Example 2 containing 97 equivalent percent calcium cations was determined. These data are set forth in Fig. 12. The final nitrogen pressure in the balance was 2.55 kPa (0.37 psia) and the residual loading was about 0.38 mmol/gram. The equilibrium nitrogen loadings at 2.55 kPa (0.37 psia) at 20°C, 0°C and -20°C, respectively, also shown in Fig. 12, were determined by extrapolation from 10.34 to 2.55 kPa (1.5 psia to 0.37 psia). The sample appears to have been chilled during desorption to a temperature of about 3°C. (d) Using the same procedure as in part (a) above, the nitrogen desorption curve for sample 2g of Example 2 containing 77 equivalent percent calcium cations was determined. These data are set forth in Fig. 13. The final nitrogen pressure in the balance was 1.93 kPa (0.28 psia) and the residual loading was about 0.07 mmol/gram. The expected equilibrium nitrogen loadings at 1.93 kPa (0.28 psia) at 20°C, 0°C and -20°C, respectively, determined by extrapolation from 10.34 to 1.93 kPa (1.5 psia to 0.28 psia), are also shown in Fig. 13. From these data the sample appears to have been chilled during desorption to a temperature of about 5°C. (e) Using the same procedure as in part (a) above, the nitrogen desorption curve for Sample 3d of Example 3 (containing 98 equivalent percent calcium cations) was determined. These data are set forth in Fig. 14. The final nitrogen pressure in the balance was 2.62 kPa (0.38 psia) and the residual loading was about 0.18 mmol/gram. The expected equilibrium nitrogen loadings at 2.41 kPa (0.35 psia) at 22°C, 30°C and -20°C, determined by extrapolation from 10.34 to 2.62 kPa (1.5 to 0.38 psia), are also shown in Fig. 14. The sample appears to have been chilled during desorption to a temperature of about -13°C. (f) Using the same procedure as in part (a) above, the nitrogen desorption curve for Sample 3b of Example 3 containing 77 equivalent percent calcium cations was determined. These data are set forth in Fig. 15. The final nitrogen pressure in the balance was 56.88 kPa (8.25 psia) and the residual loading was about 0.06 mmol/gram. From inspection of the expected equilibrium nitrogen loadings at 2.41 kPa (0.35 psia) at 22°C and 0°C, also shown in Fig. 15, the sample appears to have been chilled during desorption to a temperature of about 3°C. The expected equilibrium loadings were determined by extrapolation from 10.34 to 1.72 kPa (1.5 psia to 0.25 psia). The effectiveness of an adsorbent for air separation is measured by three parameters, i.e., nitrogen delta loading, nitrogen operational selectivity and residual nitrogen loading at the desorption pressure. Taking these parameters into account, the data of the Tables of the specification and the Figures of the drawings, including the following specific observations, clearly establish the superiority of the present invention. The adsorption data of clay-bonded X2.0 samples are given in Table III. The nitrogen residual loadings are plotted against calcium ion-exchange levels in Fig. 1. This establishes that as the calcium cation level of the zeolite adsorbent increases, the desorption of nitrogen progressively becomes more difficult, therefore the residual loading increases. At calcium levels of 90% or more, the residual nitrogen loading becomes so high, product contamination becomes a serious problem. The residual nitrogen level is also sensitive to temperature. A combination of a 90% calcium level along with an operating temperature of 0°C brings the residual nitrogen to an unacceptably high level. Since cooling always occurs in PSA processes, these data demonstrate that 90% or more calcium exchange can impair efficiency of X2.0 in more than one way. Fig. 2 gives the nitrogen delta loading between 101.3 to 10.69 kPa (14.7and 1.55 psia) of CaNaX2.0 as a function of calcium level and adsorption temperature. Initially as the calcium content increases the delta loading of nitrogen also increases. The delta loading reaches a broad maximum and starts to descend. These data demonstrate that calcium exchange levels higher than 90% or lower than 60% are desirable. Fig. 3 gives operational selectivity of X2.0 as a function of the calcium exchange level and temperature. Here is a clear example how temperature can override the influence of cation. At 40°C, the nitrogen operational selectivity increases as the calcium content increases. It peaks around 85% Ca ++ exchange and then begins to decline. At 20°C, the peak operational selectivity is in the region of 60 to 80% calcium content area. At temperatures of 0°C or lower, NaX2.0 has higher operational selectivity than does CaNaX2.0. At -20°C the nitrogen selectivity of CaNaX2.0 is substantially lower than that of NaX2.0. The adsorption data of X2.3 samples are given in Table IV. Figs. 4, 5 and 6 give residual loadings, delta loadings and operational selectivity data of X2.3 powder as a function of calcium exchange levels and adsorption temperatures. Since these samples do not contain clay, their loadings are higher than corresponding bonded samples. Results of X2.3 samples are parallel to those of X2.0. The use of an X2.3 with 90% or more of its cations in Ca ++ form and a process temperature of 0°C is clearly not desirable. For an ambient process cycle with significant temperature excursion, a CaNaX2.3 with a calcium level of at least 60%, and less than 90%, is preferred. Generally, the operational selectivity of CaNaX2.3 is lower than that of the CaNaX2.0 adsorbent. The adsorption data of bonded X2.5 beads are given in Table V. These data along with the residual loadings, delta loadings and operational selectivities plotted against calcium exchange levels in Figs. 7, 8 and 9, provide an outstanding example that the performance of a PSA adsorbent is not determined by single structure parameters. Silica-to-alumina ratio is equally as important as calcium level. The nitrogen delta loadings of X2.5 increase and the nitrogen operational selectivities decrease as the calcium levels increase. This is basically the same pattern observed in the case of X2.0 and X2.3, but with an important difference in detail. The nitrogen delta loadings of CaNaX2.5 in the 60% to 90% range are very much lower than their X2.3 and X2.0 counterparts. It is largely for this reason that CaNaX2.5 is not employed in the practice of the present invention. The data of Fig. 1 show that the residual loading or nitrogen loading at 10.7 kPa (2.55 psia) increases rapidly as the calcium content in the zeolite increases. The rate of increase is inversely proportional to the adsorption temperature. At 0°C, the residual loading of 97% calcium exchanged X2.0 is 0.79 mmol/gm which is higher than its delta loading (0.74 mmol/gm). Accordingly, it would be much more difficult to produce pure oxygen at 0°C using a CaX2.0 adsorbent. At 20°C, its residual nitrogen loading is 0.39 mmol/gm, which is high, but this adsorbent can function well using a proper process cycle. On the other hand, with a calcium level at 76 equivalent percent the nitrogen residual loadings are 0.46 mmol/gm at 0°C, which is about same as the CaX at 20°C. The residual loading of CaNaX2.0 at 20°C is 0.25 mmol/gm. CaNaX2.0 (76%) will be able to function even at 0°C and is, therefore, much favored. With reference to Fig. 2, at 0°C the nitrogen delta loading is at a maximum at a calcium content of 75%. At 20°C and 40°C, it peaks at a calcium content of about 90%. Based on the nitrogen delta loading, the 75% exchanged CaNaX2.0 would have a clear advantage over a 97% exchanged CaX2.0. In Fig. 3 it is shown that a 76% exchanged CaNaX2.0 has a higher operational selectivity than a 97% exchanged CaX2.0 at 20°C and 0°C. These data establish that the use of a CaNaX2.0 provides greater flexibility in choosing process conditions than is the case with CaX2.0. With reference to the desorption curves of Fig. 10 and Fig. 11, it can be seen that one minute into the desorption process, the residual loading on sample 1g [CaX2.0 (97% Ca)] is six times that of sample 1d [CaNaX2.0's (75% Ca)]. These data suggest that the highly exchanged zeolite will require a longer time to regenerate than the less highly exchanged composition. Another important implication of these data is that after desorption the highly exchanged material may have a significantly lower temperature than the more moderately exchanged zeolite. The drop in adsorbent temperature compounds the problems experienced with very highly Ca ++ exchanged forms of zeolite X because they are very inefficient at low temperatures. The nitrogen desorption curves of CaX2.3 (97% Ca) and the expected equilibrium adsorption capacities at 2.55 kPa (0.37 psia) are given in Fig. 12. The desorption curve of CaNaX2.3 (77% Ca) and its expected equilibrium adsorption capacities at 1.72 kPa (0.25 psia) are given in Fig. 13. The residual loading of CaX2.3 is about 0.17 mmol/gm, and its estimated temperature after desorption is about 3°C. The residual loading of CaNaX2.3 is about 0.05 mmol/gm, and the estimated temperature after desorption is about 9°C. Again, the 77% calcium-exchanged X2.3 is a more efficient adsorbent than is the 97% exchanged counterpart. The nitrogen desorption curve of CaX2.5 (97% Ca) and its expected equilibrium adsorption capacities at 262 kPa (38 psia) are given in Fig. 13. The desorption curve of CaNaX2.5 (77% Ca) and its expected adsorption capacities at 1.72 kPa (0.25 psia) are given in Fig. 14. The residual loading of CaX2.5 is about 0.17 mmol/gm, and its temperature after desorption is estimated to be about -13°C. The equilibrium loading of CaNaX2.3 is about 0.07 mmol/gm, and its temperature after desorption is estimated to be about -3°C. It is surprising to see that CaNaX2.5 has a residual loading equivalent to -3°C. However, it is consistent with the fact that CaNaX2.5 is a poor PSA adsorbent relative to CaNaX2.0 and CaNaX2.3.

Claims: An adsorbent for use in a cyclic pressure swing adsorption process for the separation of nitrogen from a mixture thereof with oxygen by selective adsorption of nitrogen, which comprises a zeolite X having a framework SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.4 and containing from 60 to 80 equivalent percent Ca ++ cations, from 10 to 40 equivalent percent Na + cations and, in addition, containing K + cations in an amount up to 10 percent, the total cation equivalency contributed by Ca ++ , Na + and K + being at least 90 percent. Cyclic process for separating nitrogen from a mixture thereof with oxygen which comprises the steps of (a) providing an adsorption bed containing an containing an absorbent wherein the adsorbent consists of a zeolite X having a framework SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.4 and containing from 60 to 80 equivalent percent Ca ++ cations, from 10 to 40 equivalent percent Na + cations and from zero to 10 percent K + cations, the total cation equivalency contributed by Ca ++ , Na + and K + being at least 90 percent; (b) passing said mixture of nitrogen and oxygen into said adsorption bed at a temperature of from -20 to 50°C until an internal bed pressure rises to the range of 13.8 to 506.8 kPa (2 to 73.5 psia) and nitrogen is selectively adsorbed on said adsorbent: (c) discharging unadsorbed oxygen as a product from the adsorption bed substantially at the adsorption pressure; and (d) decreasing the bed pressure to a final desorption pressure within the range of 101.4 to 0.7 kPa (14.7 to 0.1 psia) to desorb the adsorbed nitrogen and discharge desorbed nitrogen from the bed. Process according to claim 2 characterized in that the bed comprises a zeolite X with a SiO 2 /Al 2 O 3 molar ratio of from 2.0 to 2.35, its cation population comprising from 65 to 80 equivalent percent Ca ++ cations and from 20 to 35 equivalent percent Na + cations, said zeolite being substantially free from K + cations. A process according from claim 2 or 3 wherein the mixture of nitrogen and oxygen is air.

Inventors: CHAO CHIEN-CHUNG, CHAO, CHIEN-CHUNG
Applicants: UOP INC, UOP
Application year: 1995
Main classification: B01D53
IPC codes: B01D53, B01J20