Nitrogen sorption

Abstract: Nitrogen-sorbing and -desorbing compositions, especially compositions comprising a hexacoordinate organometallic complex, and methods of using the same are disclosed. Such compositions are useful for the selective separation of nitrogen from other gases, especially natural gas.

Description: This invention relates to the selective separation of nitrogen gas from other gases, especially from natural gas. Background of the Invention It has been estimated that 25% of the natural gas in the world contains unacceptably high levels of the non-combustive contaminant nitrogen. Efforts to remove nitrogen from natural gas have included methane sorption and various techniques of cryogenic distillation such as liquidification, turbocryogenic distillation, and "cold box" separation. All such efforts, though successful, have been relatively expensive and inefficient. There thus exists a need for a simple, efficient and low cost method of selectively removing nitrogen from natural gas. This need and others are met by the present invention, which is summarised and described in detail below. Summary of the Invention The present invention comprises a nitrogen-absorbing and -desorbing composition (also referred to herein as a "sorption material"), more particularly a composition effective in absorbing nitrogen from hydrocarbons, and a process of using the same to selectively remove nitrogen from hydrocarbon gases as hereinafter specified. Specifically, as claimed, the sorption material provided by the present invention is a composition effective in absorbing nitrogen from hydrocarbons characterised in that said composition comprises a hexacoordinate organometallic complex and a solvent selected from water, propylene carbonate, a glycol, and a glycolic oligomer, said organometallic complex consisting of a transition metal selected from Mo, W and Groups 7, 8 and 9 and at least one ligand capable of providing five coordinating atoms to said organometallic complex. In some cases, one ligand is in the axial position and is termed an "axial base", the axial base being capable of providing a coordinating atom to the organometallic complex. The process provided by the invention is a process for the removal of nitrogen from hydrocarbons comprising: (a) absorbing nitrogen from a feed stream containing essentially no oxygen and comprising nitrogen and hydrocarbon gas predominantly containing 1 to 7 carbon atoms by contacting said feed stream with the composition defined above; and (b) desorbing nitrogen from said composition to a product stream. Typically, apart from containing substantially no oxygen, the nitrogen-containing feed stream will also contain no carbon monoxide, no thiols and no sulfides. Desorption may be accomplished by temperature swing, pressure swing or a combination of the two. As the nitrogen-sorption capacity decreases over time due to decomposition of the sorption material, an optional step to improve efficiency is regeneration of its nitrogen-sorption capacity by various methods. It is acknowledged that JP-A-63042717, and an abstract thereof AN 88-089773 in Database WPIL of Derwent Publications Limited (London), refer to the use of a nitrogen-absorbing solution that comprises a selected organometallic complex dissolved in a solvent for separating nitrogen from nitrogen-containing gas such as air, but there is no suggestion of using such nitrogen-absorbing solution for separating nitrogen from hydrocarbon gases. Moreover, unlike the compositions of the present invention, the nitrogen-absorbing solution of the above-mentioned prior art documents is prepared using a solvent containing tetrahydrofuran (THF). It is also acknowledged that the patent document EP-A-0098157 published in connection with an earlier patent application filed by the present applicant discloses compositions comprising a metallo-organic compound having oxygen-complexing capability in a solution containing a solvent or solvent mixture and an axial base capable of providing a coordinating atom to the metallo-organic compound. However, these compositions are disclosed primarily only in relation to their oxygen-carrying properties, especially in the context of their use in a process for producing oxygen from an oxgyen-containing gaseous feed stream, and there is no indication in that document that the particular compositions disclosed therein would have the features claimed in the present application and be effective in absorbing nitrogen from hydrocarbons. Brief Description of Drawings FIG. 1 is a schematic of an exemplary pressure swing absorption/desorption process of the present invention. FIG. 2 is a schematic of an exemplary hybrid pressure/temperature swing absorption/desorption process of the present invention. FIG. 3 is a schematic of the exemplary process depicted in FIG. 1 wherein a pressure-reducing turbine and a regeneration loop are included. FIGS. 4 and 5 are graphs of isotherms observed for two exemplary sorption compositions of the present invention. Detailed Description of the Invention As already indicated the present invention provides nitrogen-absorbing and -desorbing material having utility in the selective removal of nitrogen from a broad class of hydrocarbon gases and specific utility in the removal of nitrogen from naturally-occurring natural gas mixtures. According to a preferred embodiment, the sorption material is a solution having two essential components: a solvent and an organometallic complex that is soluble in the solvent to ≥0.1M. In general terms, the solvent should have the following properties: hydrophilic, with a solubility parameter of ≥20 MPa ½ and preferably ≥30 MPa ½ ; either incapable of coordinating or capable of only weakly coordinating with the nitrogen-binding site of the organometallic complex; solubility of the organometallic complex therein should be ≥0.1 M , preferably ≥0.26 M , but not to exceed 95% of the solubility limit at the minimum operating temperature or that concentration that gives a solution viscosity ≤100 cps at the operating temperature; and leads to a nitrogen-absorbing solution having an apparent nitrogen solubility of ≥0.1 mol nitrogen per mol organometallic complex under the temperature and pressure of the nitrogen-containing feed as it enters a sorption column, and a substantially diminished nitrogen solubility under the temperature and pressure conditions prevailing in a desorption or stripping column. Preferably, solvents should also have low volatility (b.p. >90°C) and low toxicity. Preferred glycol solvents include ethylene glycol, propylene glycol, butylene glycol and dimethylethylene glycol. The complex comprises at least one, but not more than six, ligand(s) with a transition metal. The ligand(s) must be capable of providing five coordinating atoms to the transition metal. The ligand(s) may be monodentate, bidentate, tridentate, tetradenstate, or pentadentate, or any combination of mono-, bi-, tri-, tetra-, or pentadentate that forms a pentacoordinate complex with the metal. The organometallic complex is preferably pentacoordinate, with bound nitrogen occupying the sixth coordination site. Preferred transition metals that comprise part of the organometallic complex include some of the metals of Group 6 and the metals of Groups 7, 8 and 9, such as the early and third row transition metals Mo(0), W(0), Re(I), Re(II), Ru(II), Fe(I), Fe(II), Co(O), Co(I), Os(II), Ir(I), Rh(I) and Mn(I). The ligand that is trans to the coordinated nitrogen is termed the "axial base". Although the axial base is usually a different moiety than the equatorial ligands, it may in fact be the same. Exemplary axial bases are selected from halogens and pseudohalgens (such as hydride, cyanide and thiocyanate ions), arsines, stibnines, phosphines, phosphites, thiols, sulfides, nitrogen-containing bases, including heterocycles such as pyridines, imidazoles, amides and amines, sulfur-containing heterocycles such as thiophenes, carbon monoxide, nitrogen, nitrous oxide, hydroxy, alkoxy, arylkoxy, hydrocarbon residues such as alkyl, aryl and olefinic groups. The axial base may also be covalently attached to one or more of the equatorial ligands through a bridging group. A tabulation of suitable axial bases is set forth in Table 1. Table 2 contains definitions of the R substituents of both the axial bases and the polydentate ligands, while Table 3 contains definitions of the R' bridging groups of the polydentate ligands. Substituent Group Type Definition of R A alkyl and substituted alkyl 1°, 2°, 3° and cyclic contg. 1-10 carbons where substituents are selected from halo, hydroxy, cyano, amido, amino, mono- and dialkylamino, mono- and diaryl amino, mercapto, sulfonyloxy, alkoxy, thioalkoxy, aryloxy, thioaryloxy, carboxy, alkoxycarbonyl, alkyl- and arylsulfinyl, alkyl- and arylphospho, alkyl- and arylphosphono, substituted and unsubstituted aryls, including phenyl, biphenyl, naphthyl, substituted and unsubstituted N- and S-contg. heteroaryl, including pyridyl, pyrryl, piperidinyl, piperazyl, thienyl, tetra-hydrothioenyl, and thiazolyl groups B aryl and substituted aryl phenyl, biphenyl, naphthyl and anthracenyl where substituents are selected from those in this Table, Substituent Group A C heterocycles and substituted heterocycles N- and S-contg. heterocycles as defined in Table 1, Groups 3 and 4, where substituents are selected from those in this Table, Substituent Group A Bridging Group Type Definition of R' I alkylene, substituted alkylene, alkenylene and substituted alkenylene 1°, 2°, 3° and cyclic, contg. 1-10 carbons where bridging hydrocarbon chain contains 1-4 carbons and where substituents are selected from those in Table 2, Substituent Group A II arylene and substituted arylene as defined in Table 2, Substituent Group B, and contg two coordinating/chelating groups selected from N, P, S, As and Sb in the 1,2-positions for phenyl; in the 1,2-, 1,8- or 2,3-positions for naphthyl; in the 2,2'-, 2,3- or 3,4-positions for biphenyl; or in the 1,2-, 2,3- or 1,9-positions for anthracenyl III heterocycles and substituted heterocycles as defined in Table 2, Substituent Group C, and contg. two coordinating/chelating groups selected from N, P, S, As and Sb in any two adjacent positions Suitable monodentate equatorial ligands include the following four groupings of organic compounds: 1. arsines, amines, phosphines and stibnines of the structure where Z is selected from As, N, P and Sb and each R is independently selected from -H or any of the substituents recited in Table 2, Substituent Group A, B or C (as a group, the three R substituents may comprise any combination of -H or the substituents shown in Table 2); 2. thiols and sulfides of the structure R - S - R where R is as defined above; 3. halogens and the pseudohalogens H - , CN - and SCN - ; and 4. carbon monoxide and nitrous oxide. Suitable bidentate equatorial ligands include the following four groups of organic compounds: 1. amines, arsines, phosphines and stibnines of the structure where R and Z are as defined above and R' is any of the bridging ligands set forth in Table 3; 2. phosphites of the structure where R and R' are as defined above; 3. thiols and sulfides of the structure R-S-R'-S-R where R and R' are as defined above; and 4. substituted and unsubstituted nitrogen-and sulfur -containing heterocycles as defined in Table 1, Groups 3 and 4. Suitable tridentate equatorial ligands include the following four groups of organic compounds: 1. amines, arsines, phosphines and stibnines of the structure where R, R' and Z are as defined above; 2. phosphites of the structure where R and R' are as defined above; 3. thiols and sulfides of the structure R-S-R'-S-R'-S-R where R and R' are as defined above; and 4. substituted and unsubstituted nitrogen-and sulfur -containing heterocycles as defined in Table 1, Groups 3 and 4. Suitable tetradentate equatorial ligands include the following six groups of organic compounds: 1. amines, arsines, phosphines, and stibnines of the structure where Z, R and R' are as defined above; 2. phosphites of the structure where R and R' are as defined above; 3. thiols and sulfides of the structure where R and R' are as defined above. 4. substituted and unsubstituted nitrogen-and sulfur -containing heterocycles as defined in Table 1, Groups 3 and 4. 5. substituted and unsubstituted porphyrins of the structure where R is as defined above; and 6. substituted and unsubstituted phthalocyanines of the structure where R is as defined above. Structural drawings of various equatorial ligands ("L"), where the ligand trans to the bound nitrogen (N 2 ) is an axial base ("B") coordinated to the metal ("M") are shown below: The ligands (including the axial base) may be in any combination such that they provide 5 coordinating atoms to the complex. Thus, for example, any of the following combinations of ligands are suitable: 5 monodentates; 3 monodentates and 1 bidentate; 1 each of a bi- and tridentate; 1 each of a mono- and a tetradentate; 2 monodentates and 1 tridentate; and 1 pentadentate. The nitrogen sorption material may be used in any of a pressure swing absorption (PSA), a temperature swing absorption (TSA) or a hybrid combination of PSA and TSA. In general, with the nitrogen sorption material in the form of a solution, it is preferably used in a PSA mode. In a PSA mode, the difference in nitrogen partial pressures between the absorption and desorption steps is preferably in the range of 68.94 to 2757.6 kPa (10 to 400 psi). Nitrogen partial pressure in the desorption step may also be reduced by the use of an inert sweep gas, such as carbon, dioxide, argon, hydrogen, helium or methane, preferably in a countercurrent flow mode. Sweep gas may also effectively be generated in situ by the release of other gases (such as methane or other hydrocarbons) absorbed in the solution or by solvent vapor; this release of other sorbed gases effectively lowers the partial pressure of nitrogen. In terms of total pressure, the absorption step is preferably conducted at a total pressure that is at least 20 times the total pressure of the desorption step. When used in a TSA mode, the preferred temperature differential between the absorption and desorption steps is in the range of 20 to 100°C for economic efficiency to be realized. The feed gas preferably comprises a mixture of nitrogen and other gases, typically methane and other hydrocarbons, and as well as containing essentially no oxygen the mixture preferably contains no carbon monoxide, no thiols and no sulfides. Preferred limits on such impurities are such that the partial pressures of the gases are as follows: oxygen 56.894 kPa (1 psi), preferably 6.894 Pa (10 -3 psi); carbon monoxide ≤ 68.94 kPa (10 psi); sulfides and thiols ≤ 6.894 Pa (10 -3 psi). Notwithstanding these preferred limits, in some cases the nitrogen sorption material may be relatively unaffected by the presence of such impurities and so the feed gas may contain substantial amounts, say, up to 10 vol%, of the same. In general, non-nitrogen components should be soluble in the solvent to a concentration that is less than twice the solubility of the organometallic complex. The feed may be at virtually any temperature in the range of -20°C to 100°C although in certain cases, mentioned below, higher temperatures may also be used. In general, the preferred temperature range is 0°C to 100°C. The amount of nitrogen in the feed stream may be anywhere from 0.1 to 80 vol%. Preferred applications in accordance with the invention include mixtures of nitrogen with hydrocarbons containing from 1 to 7 carbons, including natural gas, and with hydrocarbons from partial oxidation of hydrocarbons containing from 1 to 7 carbon atoms (from the oxidation of coal and from the oxidative coupling of hydrocarbons). The range of the temperature of the feed may be from 0°C to 200°C, preferably 20°C to 150°C. The feed may be fed at a pressure of anywhere from 137.88 kPa (20 psi) to 13788 kPa (2000 psi). Over time, the nitrogen-sorbing capacity of the solution may decrease due to a formal oxidation of the metal atom in the organometallic complex. The nitrogen-absorbing capability of the solution may be periodically regenerated by a variety of techniques, including: (1) formally reducing the metal by heating the solution to 30°C to 180°C while avoiding oxidizing conditions, preferably in the presence of a reducing agent such as hydrogen, magnesium, iron or thiosulfate ion; (2) stripping the solvent from the solution and then recrystallizing the residual organometallic complex from a suitable solvent under a nitrogen or other inert gas atmosphere; and (3) demetallating the organometallic complex in solution by the addition of a strong acid, extracting the oxidized transition metal into an immiscible organic solvent, then coordination of the reduced transition metal with the solution of the equatorial ligand(s) and axial base, and recrystallizing the regenerated organometallic complex. In connection with the first regeneration method mentioned above, oxidizing conditions may be avoided by heating the solution (a) under a vacuum of from 2.666 to 266.64 kPa (0.2 to 20 cmHg) for about 1 to 48 hours, (b) in an inert atmosphere such as nitrogen or argon for about 1 to 72 hours, or (c) in a reducing atmosphere such as hydrogen for from about 1 to 72 hours, with or without the presence of a reduction catalyst such as a platinum group metal. In connection with the second regeneration method, the inactive organometallic complex may be isolated from the solvent by vacuum or atmospheric distillation of the solvent, and the residual organo-metallic complexes recrystallized from an appropriate solvent. In connection with the third method of regeneration, suitable strong acids include hydrochloric acid, sulfuric acid, and trifluoroacetic acid. The oxidized metal may be extracted into an immiscible organic solvent, such as toluene and other aromatic solvents, and hexane and other aliphatic solvents, by addition of an organic-soluble metal extractant, such as dialkylphosphoric acids, alkylamines, quaternary alkylamines, and alkyl-β-diketones, to the aromatic or aliphatic solvent. Suitable solvents for recrystallization of the organometallic complex include water, methanol, ethanol, tetrahydrofuran, and acetonitrile. Referring now to the drawings, wherein like numerals refer to the same elements, use of the solution of the present invention in a PSA mode is depicted in FIG. 1. There, a nitrogen-containing feed 10 is introduced into a conventional gas-liquid absorption column 20 so that the gas is efficiently contacted with the solution of the present invention. Within the absorption column 20, nitrogen is selectively absorbed by the solution, resulting in a reduction in the nitrogen concentration in the "product" gas 25 exiting the column (it being understood that virtually any gas other than nitrogen, depending upon the desired separation, could be regarded as the product gas). The residence time of the solvent in the absorption column 20 is on the order of a few minutes and generally should be sufficiently long to achieve nitrogen binding to at least 10 mol% of the organometallic absorbent. The column should be sized sufficiently to accommodate the requisite volume and flow rate of liquid absorbent to have sufficient contact time for nitrogen to be absorbed by the liquid. In place of the absorption column 20, other gas-liquid contactors may be utilized, such as membrane contactors in the form of hollow fiber modules. The nitrogen-complexed liquid absorbent 28 is passed to a stripping column 40 in which nitrogen is desorbed from the liquid absorbent. For nitrogen desorption to occur in the stripping column, the partial pressure of nitrogen in the nitrogen-containing stream 45 exiting the stripping column 40 must be less than the partial pressure of nitrogen in the product stream 25 exiting the absorption column 20. This condition is met by operating the stripping column 40 at a reduced pressure relative to the absorption column 20 (typically near 0 psig total pressure) or by using a sweep stream 35 to maintain low nitrogen partial pressures in the nitrogen-containing stream 45 exiting the stripping column 40. The nitrogen-containing stream 45 desorbed from the liquid absorbent exits the stripping column 40 at substantially the same pressure as that prevailing in the stripping column, which is typically near 0 psig total pressure. In some cases the desorbed nitrogen from the nitrogen-containing stream 45 may be the end product of the separation process. After nitrogen is desorbed from the liquid absorbent in the stripping column 40, the nitrogen-stripped liquid absorbent 48 is returned to the absorption column 20 by use of a pump 30, and the cycle is repeated. Use of the nitrogen-sorbing and -desorbing solution of the present invention in a hybrid PSA/TSA mode is shown schematically in FIG. 2. There, the system is operated in generally the same manner as described for FIG. 1, except that the stripping column 40 is operated at an elevated temperature relative to the absorption column 20, the addition of heat to the stripping column 40 being depicted schematically by the symbol "+Q". Alternatively, the absorption column 20 may be cooled relative to the stripping column 40, this being schematically depicted by the symbol "-Q". This hybrid mode of operation is useful in compensating for the fact that the nitrogen-binding capacity of the liquid absorbent for a given nitrogen partial pressure decreases with increasing temperature inasmuch as the nitrogen-binding is typically a somewhat exothermic reaction. As a result, the nitrogen partial pressure in equilibrium with the nitrogen-containing absorbent will increase with increasing temperature. For nitrogen desorption to occur in the stripping column 40, the concentration in the absorbent liquid in equilibrium with product gas 25 exiting the absorption column 20 at the temperature and pressure prevailing therein must exceed the concentration of nitrogen in the absorbent in equilibrium with the nitrogen in nitrogen-containing stream 45 at the temperature and pressure prevailing in the stripping column 40. The advantage of the hybrid PSA/TSA mode over the purely PSA mode is that in the former, nitrogen desorption can be achieved in the stripping column 40 at nitrogen partial pressures greater than those allowed in the strictly PSA mode. As with the PSA mode, the hybrid PSA/TSA mode may be used to achieve nitrogen desorption in the stripping column 40 by either operating the stripping column at reduced pressure relative to the absorption column or by the use of a sweep gas. However, since the stripping column is at a higher temperature than the absorption column, the stripping column need not be at a lower pressure but may be at the same or even higher pressure than the absorption column. Another advantage of operating the stripping column at elevated temperature is that an increase in the rate of nitrogen desorption from the liquid absorbent occurs, resulting in a decrease in the residence time required for the liquid absorbent in the stripping column. FIG. 3 depicts the inclusion of a regeneration loop 50 wherein the nitrogen-stripped liquid sorbent 48 is treated by one of the methods described above to regenerate its nitrogen-sorption capacity, as well as the inclusion of a pressure-reducing turbine 38 to recover energy otherwise lost, the energy being used to drive the liquid pump 30. A preferred type of pressure-reducing or power recovery turbine is that which is commercially available from Sulzer Bingham of Portland, Oregon. Example 1 A 0.25 M solution of the organometallic complex [Ru(H 2 0)(Hedta)] - in water (as the potassium salt) was used to determine nitrogen-binding isotherms at 21°C and at 41°C (Hedta is monoprotonated ethylene diamine tetraacetate). This was accomplished by measuring the uptake of nitrogen by the solution over a range of nitrogen pressures. The resulting isotherms are shown in FIG. 4. From these isotherms, the equilibrium constant of nitrogen binding is calculated to be 0.08 (psi-M) -1 at 21°C and 0.024 (psi-M) -1 at 41°C. These equilibrium constants are based on the following assumed nitrogen-binding reaction: 2[Ru(H 2 0)(Hedta)] - +N 2 ⇄([Ru(N 2 )(Hedta)] 2 N 2 ) -2 +2H 2 0. These data show that at 21°C and high nitrogen pressures, i.e. 2068.2 to 2412.9 kPa (300 to 350 psi), the solution of [Ru(H 2 0)(Hedta)] - absorbs approximately 0.5 mmole of nitrogen per mmole of the complex. However, at 21°C and low nitrogen pressure, i.e. < 344.7 kPa (<50 psi), the solution absorbs <0.2 mole nitrogen per mmole of the complex. Thus, an aqueous solution of this organometallic complex can be used to remove nitrogen from a high-pressure gas stream by first permitting the solution to absorb nitrogen at high pressure, then pumping the nitrogen-laden solution to a stripping column at low pressure to allow nitrogen to desorb from the solution. For example, at a solution temperature of about 21°C, a swing in nitrogen partial pressure from 2412.9 kPa (350 psi) in the absorption stage to 344.7 kPa (50 psi) in the desorption stage will result in the net removal of more than 0.3 mmole of nitrogen per mmole of [Ru (Hedta)] - . Referring again to FIG. 4, the 41°C isotherm is shifted below the 21°C isotherm because coordination of nitrogen to the organometallic complex is an exothermic process, i.e., as the temperature increases, the fraction of nitrogen coordinated to the organometallic complex decreases. This property may be used to increase the amount of nitrogen that is desorbed from the nitrogen-laden solution. Accordingly, a hybrid PSA-TSA process may be used to remove nitrogen from a gas stream by permitting the complex-containing solution to absorb nitrogen at high pressure at about 21°C, removing the nitrogen-laden solution, and heating it to about 41°C, then pumping the nitrogen-laden solution to a stripping column at low pressure, thereby allowing nitrogen to desorb from the solution. For example, by maintaining the nitrogen partial pressure at about 2412.9 kPa (350 psi) and the temperature at 21°C in the absorption column and at about 344.7 kPa (50 psi) and 40°C in the stripping column, about 0.45 mmole nitrogen per mmol [Ru (Hedta)] - may be removed from the feed gas. Example 2 The nitrogen-binding isotherm at 21°C of a 0.02 M solution of the organometallic complex [Fe(H)(diphos) 2 ] + (diphos = Ph 2 PCH 2 CH 2 PPh 2 ) was determined. This was accomplished by measuring, as a function of nitrogen pressure, the intensity of the infrared absorption band corresponding to the nitrogen-nitrogen stretch at 2122 cm -1 . The results are shown in FIG. 5. From this isotherm the equilibrium constant for nitrogen-binding is calculated to be 0.15 (psi-M) -1 . The value of the equilibrium constant is based on the following assumed nitrogen-binding reaction: [Fe(H)(diphos) 2 ] + +N 2 ⇄[Fe(H)(diphos) 2 (N 2 )] + . Since [Fe(H)(diphos) 2 ] binds nitrogen more tightly than [Ru(H 2 0)(Hedta)] - , the nitrogen can be desorbed only at relatively low nitrogen partial pressure and/or elevated temperatures. For example, to achieve a net removal of 0.5 mmole nitrogen per mmole [Fe(H)(diphos) 2 ] + at a temperature of about 21°C, the nitrogen partial pressure in the desorption column would have to be about 48.26 kPa absolute (7 psia) or less given a nitrogen pressure in the absorption column of at least 1378.8 kPa relative to atmospheric pressure (200 psig). As is the case with [Ru(H 2 0)(Hedta)] - , desorption of nitrogen from a solution of [Fe(H)(diphos) 2 ] + can be achieved at higher nitrogen pressures if the solution is heated (e.g., to about 41°C) during the desorption of nitrogen. Example 3 To demonstrate that nitrogen is selectively absorbed from a gas mixture containing nitrogen and methane, a 0.36 M (7.2 mmole) aqueous solution of the organometallic complex [Ru(H 2 0)(Hedta)] - (as the potassium salt) was exposed to a 7.5% nitrogen-containing nitrogen/methane gas mixture at 3571.09 kPa (518 psi). Nitrogen partial pressure loss demonstrated that approximately 0.24 mmole of nitrogen gas was complexed or absorbed by the complex-containing solution. Isolation of the remainder of the gas mixture and analysis by gas liquid chromatography demonstrated its composition to be 7.0±0.1% nitrogen, indicating that 0.5% (0.19 mmole) nitrogen was desorbed from the solution. Example 4 The organometallic complex-containing solution of the present invention was demonstrated to be regenerable. A 0.4 M aqueous solution of the organometallic complex [Ru(H 2 0)(Hedta)] - was exposed to air for 24 hours. Aerobic oxidation of [Ru(H 2 0)(Hedta)] - is reported in the literature to yield [Ru(H 2 0)(Hedta)], which does not absorb nitrogen. That is, contact with air results in oxidation of Ru from the +2 to the +3 oxidation state. Subsequently the oxidized solution was contacted with the reducing agent magnesium to regenerate [Ru(H 2 0)(Hedta)] - . The regenerated solution was found to reversibly absorb nitrogen according to the binding isotherm shown in FIG. 4 and also to selectively absorb nitrogen from N 2 /CH 4 as described in Example 3. The terms and expressions which have been employed in the foregoing specification are used therein as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding equivalents of the features shown and described or portions thereof.

Claims: A composition effective in absorbing nitrogen from hydrocarbons characterized in that said composition comprises a hexacoordinate organometallic complex and a solvent selected from water, propylene carbonate, a glycol, and a glycolic oligomer, said organometallic complex consisting of a transition metal selected from Mo, W and Groups 7, 8 and 9 and at least one ligand capable of providing five coordinating atoms to said organometallic complex. The composition of claim 1 wherein said at least one ligand comprises a ligand selected from a monodentate, a bidentate, a tridentate, a tetradentate, and a pentadentate ligand. The composition of claim 1 wherein said transition metal is selected from the group consisting of Mo(0), W(0), Re(I), Re(II), Ru(II), Fe(I), Fe(II), Co(O), Co(I), Os(II), Ir(I), Rh(I) and Mn(I). The composition of claim 1 wherein said organometallic complex includes more than one ligand, one of which is an axial base selected from the group consisting of halogens, hydride, nitrogen, carbon monoxide, nitrogen-containing bases, phosphines, pyridines, and imidazoles. The composition of claim 1 wherein said at least one ligand is monodentate and is selected from the group consisting of halogens, hydrides, carbon monoxide, amines, and phosphines. The composition of claim 1 wherein said at least one ligand is bidentate and is selected from the group consisting of phosphines, phosphites, thiols, sulfides, and amines. The composition of claim 1 wherein said at least one ligand is tridentate and is selected from the group consisting of phosphines and amines. The composition of claim 1 wherein said at least one ligand is tetradentate and is selected from the group consisting of phosphines and amines. The composition of claim 1 wherein said at least one ligand is pentadentate and is selected from the group consisting of phosphines and amines. A process for the removal of nitrogen from hydrocarbons comprising: (a) absorbing nitrogen from a feed stream containing essentially no oxygen and comprising nitrogen and hydrocarbon gas predominantly containing 1 to 7 carbon atoms by contacting said feed stream with the composition of claim 1; and (b) desorbing nitrogen from said composition to a product stream. The process of claim 10 wherein said hydrocarbon gas is natural gas. The process of claim 10 wherein step (a) is conducted at a lower temperature than step (b). The process of claim 12 wherein the difference between the temperatures of steps(a) and (b) is 20 to 100°C. The process of claim 10 wherein step (a) is conducted at a nitrogen partial pressure that is greater than the nitrogen partial pressure of step (b). The process of claim 14 wherein the difference between the nitrogen partial pressures of steps (a) and (b) is 68.94 to 2757.6 kPa (10 to 4000 psi). The process of claim 10 wherein step (a) is conducted at a total pressure that is at least 20 times the total pressure in step (b). The process of claim 14 wherein step (a) is conducted at a lower temperature than the temperature of step(b). The process of claim 17 wherein the difference between the temperatures of steps (a) and (b) is 20 to 100°C. The process of claim 10 wherein step (b) is conducted with a sweep gas. The process of claim 10, including periodic regeneration of the nitrogen-absorbing capability of said solution. The process of claim 20 wherein said regeneration is accomplished by heating said solution in an inert atmosphere. The process of claim 20 wherein said regeneration is accomplished by heating said solution in the presence of a reducing agent.

Inventors: BABCOCK WALTER C, EDLUND DAVID J, FRIESEN DWAYNE T, MILLER WARREN K, BABCOCK, WALTER, C., EDLUND, DAVID J., FRIESEN, DWAYNE T., MILLER, WARREN K.
Applicants: BEND RES INC, BEND RESEARCH, INC.
Application year: 1992
Main classification: B01D53
IPC codes: C01B21, C07F15, B01D53, B01J20, C07F9, C10K1