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Sulfur resistant/tolerant adsorbents useful for separating olefins from paraffins in a cracked gas stream including hydrogen sulfide. The method comprises the steps of contacting the gaseous mixture with an adsorbent which preferentially adsorbs the alkene, at a selected temperature and pressure, th

Sulfur resistant/tolerant adsorbents useful for separating olefins from paraffins in a cracked gas stream including hydrogen sulfide. The method comprises the steps of contacting the gaseous mixture with an adsorbent which preferentially adsorbs the alkene, at a selected temperature and pressure, thereby producing a non-adsorbed component and an alkene-rich adsorbed component; the adsorbent comprising a carrier having a surface area, the carrier having been impregnated with a silver compound by incipient wetness, the silver compound releasably retaining the alkene; and changing at least one of the pressure and temperature to thereby release the alkene-rich component from the adsorbent. The adsorbent substantially maintains its adsorbent capacity and preference for the alkene in the presence of the sulfur compound. Sulfur resistant/tolerant adsorbents useful for selectively separating dienes from a mixture, particularly one containing mono-olefins and hydrogen sulfide, are also disclosed.

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1. A method of separating gaseous alkene selected from the group consisting of ethylene, propylene and mixtures thereof, from a gaseous mixture including the alkene and a sulfur, the hydrogen sulfide present in amounts normally present in conventional cracked gas streams, the method comprising the s

1. A method of separating gaseous alkene selected from the group consisting of ethylene, propylene and mixtures thereof, from a gaseous mixture including the alkene and a sulfur, the hydrogen sulfide present in amounts normally present in conventional cracked gas streams, the method comprising the steps of:contacting the gaseous mixture with an adsorbent which preferentially adsorbs the alkene, at a selected temperature and pressure, thereby producing a non-adsorbed component and an alkene-rich adsorbed component; the adsorbent comprising a carrier having a surface area, the carrier having a monolayer of a silver compound dispersed on substantially the entire surface area, the silver compound releasably retaining the alkene; and the carrier comprising a plurality of pores having a pore size greater than the effective molecular diameter of the alkene; and changing at least one of the pressure and temperature to thereby release the alkene-rich component from the adsorbent; wherein the adsorbent substantially maintains its adsorbent capacity and preference for the alkene in the presence of the hydrogen sulfide. 2. The method as defined in claim 1 wherein the silver compound comprising silver nitrate (AgNO3), and the carrier is silica (SiO2).3. The method as defined in claim 1 wherein the silver compound comprising a silver salt, and wherein the salt is selected from the group consisting of acetate, benzoate, bromate, chlorate, perchlorate, chlorite, citrate, fluoride, nitrate, nitrite, sulfate, and mixtures thereof.4. The method as defined in claim 1 wherein the carrier has a BET surface area greater than about 50 square meters per gram and up to about 2,000 square meters per gram, and comprises a plurality of pores having a pore size greater than about 3 angstroms and up to about 10 microns.5. The method as defined in claim 1 wherein the carrier is a high surface area support selected from the group consisting of refractory inorganic oxide, molecular sieve, activated carbon, and mixtures thereof.6. The method as defined in claim 5 wherein the refractory inorganic oxide is selected from the group consisting of pillared clay, alumina and silica.7. The method as defined in claim 1 wherein the silver compound comprising a silver (I) halide, and the carrier is silica.8. The method as defined in claim 1 wherein the selected pressure of preferential adsorption is a first pressure, and the pressure of release is a second pressure less than the first pressure, and wherein the first pressure is in a range of about 1 atmosphere to about 35 atmospheres, and further wherein the second pressure is in a range of about 0.01 atm to about 5 atm.9. The method as defined in claim 1 wherein the selected temperature of preferential adsorption is a first temperature, and the temperature of release is a second temperature greater than the first temperature, and wherein the first temperature is in a range of about O° C. to about 50° C., and further wherein the second temperature is in a range of about 70° C. to about 200° C.10. The method as defined in claim 1 wherein the retaining of the alkene is accomplished by formation of π-complexation bonds between the silver compound and the alkene.11. A method for separating a diene from a mixture including the diene and hydrogen sulfide, the hydrogen sulfide present in amounts normally present in conventional cracked gas streams, the method comprising the step of:contacting the mixture with an adsorbent which preferentially adsorbs the diene, at a selected temperature and pressure, thereby producing a non-adsorbed component and a diene-rich adsorbed component, wherein the adsorbent comprises an ion-exchanged zeolite selected from the group consisting of zeolite X, zeolite Y, zeolite LSX, and mixtures thereof, the zeolite having exchangeable cationic sites, and a majority of the sites having silver cation or copper cation present, and wherein the preferential adsorption occurs by π-complexation, and further wherein the adsorbent substantially maintains its adsorbent capacity and preference for the diene in the presence of the hydrogen sulfide. 12. The method as defined in claim 11 wherein the diene is selected from the group consisting of butadiene, hexadiene, octadiene and mixtures, thereof, and wherein the method further comprises the step of changing at least one of the pressure and temperature to thereby release the diene rich component from the adsorbent.13. The method as defined in claim 11 wherein the diene is 1,3-butadiene, and wherein the mixture includes 1,3-butadiene and at least one other C4 unsaturated compound.14. The method as defined in claim 11 wherein the majority of the cationic sites of the ion-exchanged zeolite contain the silver cation.15. The method as defined in claim 11 wherein the majority of the cationic sites of the ion-exchanged zeolite contain the copper cation.16. The method as defined in claim 11 wherein the mixture comprises at least one mono-olefin having as many carbon atoms as the diene, wherein the diene is selected from the group consisting of butadiene, hexadien, octadiene, and mixtures thereof; and wherein the mono-olefin is selected from the group consisting of butene, hexene, octene, and mixtures thereof.17. The method as defined in claim 16 wherein the mono-olefin is butene and the diene is butadiene.18. The method as defined in claim 16 wherein the mixture comprises the mono-olefin in a gaseous state and saturated with the diene.19. The method as defined in claim 11 wherein essentially all cationic sites of the ion-exchanged zeolite contain the silver cation.20. The method as defined in claim 12 wherein the selected pressure of preferential adsorption is a first pressure, and the pressure of release is a second pressure less than the first pressure, wherein the first pressure is in a range of about 1 atmosphere to about 35 atmosphere, and wherein the second pressure is in a range of about 0.01 atmosphere to about 5 atmospheres.21. The method as defined in claim 12 wherein the selected temperature of preferential adsorption is a first temperature, and the temperature of release is a second temperature greater than the first temperature, wherein the first temperature is in a range of about O° C. to about 150° C., and wherein the second temperature is in a range of about 70° C. to about 250° C.22. A method of separating gaseous alkene selected from the group consisting of ethylene, propylene and mixtures thereof, from a gaseous mixture including the alkene and a sulfur compound, the method comprising the steps of:contacting the gaseous mixture with an adsorbent which preferentially adsorbs the alkene, at a selected temperature and pressure, thereby producing a non-adsorbed component and an alkene-rich adsorbed component; the adsorbent comprising a carrier having a surface area, the carrier having a monolayer of a silver compound dispersed on substantially the entire surface area, the silver compound releasably retaining the alkene; and the carrier comprising a plurality of pores having a pore size greater than the effective molecular diameter of the alkene; and changing at least one of the pressure and temperature to thereby release the alkene-rich component from the adsorbent; wherein the adsorbent substantially maintains its adsorbent capacity and preference for the alkene in the presence of the sulfur compound, wherein the sulfur compound is hydrogen sulfide, and wherein the hydrogen sulfide is present in amounts up to about 66 mole %. 23. The method as defined in claim 11 wherein the hydrogen sulfide is present in amounts up to about 66 mole %.24. A method for separating a diene from a mixture including the diene and hydrogen sulfide, the hydrogen sulfide present in amounts normally present in conventional cracked gas streams, the method comprising the step of:contacting the mixture with an adsorbent which preferentially adsorbs the diene, at a selected temperature and pressure, thereby producing a non-adsorbed component and a diene-rich adsorbed component, wherein the adsorbent comprises an ion-exchanged zeolite selected from the group consisting of zeolite X, zeolite Y, zeolite LSX, and mixtures thereof, the zeolite having exchangeable cationic sites, and at least some of the sites having silver cation or copper cation present, and wherein the preferential adsorption occurs by π-complexation, and further wherein the adsorbent substantially maintains its adsorbent capacity and preference for the diene in the presence of the hydrogen sulfide. 25. The method as defined in claim 24 wherein the diene is selected from the group consisting of butadiene, hexadiene, octadiene and mixtures thereof, and wherein the method further comprises the step of changing at least one of the pressure and temperature to thereby release the diene-rich component from the adsorbent.26. The method as defined in claim 24 wherein the diene is 1,3-butadiene, and wherein the mixture includes 1,3-butadiene and at least one other C4 unsaturated compound.27. The method as defined in claim 24 wherein a majority of the cationic sites of the ion-changed zeolite contain the silver cation.28. The method as defined in claim 24 wherein a majority of the cationic sites of the ion-exchanged zeolite contain the copper cation.29. The method as defined in claim 24 wherein the mixture comprises at least one mono-olefin having as many carbon atoms as the diene, wherein the diene is selected from the group consisting of butadiene, hexadiene, octadiene, and mixtures thereof; and wherein the mono-olefin is selected from the group consisting of butene, hexene, octene, and mixtures thereof.30. The method as defined in claim 29 wherein the mono-olefin is butene and the diene is butadiene.31. The method as defined in claim 29 wherein the mixture comprises the mono-olefin in a gaseous state and saturated with the diene.32. The method as defined in claim 24 wherein essentially all cationic sites of the ion-exchanged zeolite contain the silver cation.33. The method as defined in claim 25 wherein the selected pressure of preferential adsorption is a first pressure, and the pressure of release is a second pressure less than the first pressure, wherein the first pressure is in a range of about 1 atmosphere to about 35 atmospheres, and wherein the second pressure is in a range of about 0.01 atmosphere to about 5 atmospheres.34. The method as defined in claim 25 wherein the selected temperature of preferential adsorption is a first temperature, and the temperature of release is a second temperature greater than the first temperature, wherein the first temperature is in a range of about O° C. to about 150° C., and wherein the second temperature is in a range of about 70° C. to about 250° C.35. The method as defined in claim 24 wherein the at least some of the sites have silver cation present.36. The method as defined in claim 24 wherein the at least some of the sites have copper cation present.37. The method as defined in claim 24 wherein essentially all cationic sites of the ion-exchanged zeolite contain the copper cation.38. A method for separating a diene from a mixture including the diene and hydrogen sulfide, the hydrogen sulfide present in amounts normally present in conventional cracked gas streams, wherein the diene is selected from the group consisting of butadiene, hexadiene, octadiene and mixtures thereof, wherein the mixture comprises at least one mono-olefin having as many carbon atoms as the diene, and wherein the mono-olefin is selected from the group consisting of butene, hexane, octene, and mixtures thereof, the method comprising the steps of:contacting the mixture with an adsorbent which preferentially adsorbs the diene, at a selected temperature and pressure, thereby producing a non-adsorbed component and a diene-rich adsorbed component, wherein the adsorbent comprises an ion-exchanged zeolite selected from the group consisting of zeolite X, zeolite Y, zeolite LSX, and mixtures thereof, the zeolite having exchangeable cationic sites, and at least some of the sites having silver cation or copper cation present, and wherein the preferential adsorption occurs by π-complexation, and further wherein the adsorbent substantially maintains its absorbent capacity and preference for the diene in the presence of the hydrogen sulfide; changing at least one of the pressure and temperature to thereby release the diene-rich component from the adsorbent, wherein the selected pressure of preferential adsorption is a first pressure, and the pressure of release is a second pressure less than the first pressure, wherein the first pressure is in a range of about 1 atmosphere to about 35 atmospheres, and wherein the second pressure is in a range of about 0.01 atmosphere to about 5 atmospheres; and wherein the selected temperature of preferential adsorption is a first temperature, and the temperature of release is a second temperature greater than the first temperature, wherein the first temperature is in a range of about O° C. to about 150° C., and wherein the second temperature is in a range of about 70° C. to about 250° C. 39. The method as defined in claim 38 wherein the mono-olefin is butene and the diene is butadiene.40. The method as defined in claim 38 wherein the mixture comprises the mono-olefin in a gaseous state and saturated with the diene.41. The method as defined in claim 38 wherein a majority of the sites have silver cation present.42. The method as defined in claim 38 wherein a majority of the sites have copper cation present.43. The method as defined in claim 38 wherein essentially all cationic sites of the ion-exchanged zeolite contain the copper cation.44. The method as defined in claim 38 wherein essentially all cationic sites of the ion-exchanged zeolite contain the silver cation.45. The method as defined in claim 1 wherein the gaseous mixture is contained in a conventional cracked gas stream before any desulfurizing distillation steps.46. The method as defined in claim 11 wherein the gaseous mixture is contained in a conventional cracked gas stream before any desulfurizing distillation steps.47. The method as defined in claim 24 wherein the gaseous mixture is contained in a conventional cracked gas stream before any desulfurizing distillation steps.48. The method as defined in claim 38 wherein the gaseous mixture is contained in a conventional cracked gas stream before any desulfurizing distillation steps.