SELECTIVE EXTRACTION OF ARGON FROM ETHYLENE OXIDE RECYCLE STREAM

Abstract: In the production of ethylene oxide by the reaction of ethylene and oxygen with subsequent recovery of the ethylene oxide so formed and recycle of a gas mixture containing argon and unreacted ethylene, the argon concen­ tration in the cycle gas is reduced without significant loss of ethylene by use of a semi-permeable membrane unit.

Description: BACKGROUND OF THE INVENTION Field of the Invention This invention relates to an improvement in the process for the production of ethylene oxide through the silver catalyzed vapor phase oxidation of ethylene and, more particular ly, to an economic process for producing ethylene oxide which minimizes unreacted ethylene losses through the use of semipermeable membrane separation units, thereby permitting an effective, selective removal of argon diluents from the process cycle gas, without significant 'ethylene losses. Description of the Prior Art The production of ethylene oxide is one of the most important commercial reactions in the world, with a current annual production of about eight million tons/year worldwide. Frequently the operation of a process of this magnitude within the realm of commercial practicality can often depend upon the ability to increase, even by only relatively small amounts, the ethylene oxide yield or, conversely, the ability to reduce, even by only relatively small amounts, the costs of a variety of essential elements of the process. In one major embodiment of the process, the oxygen supplied for reacting with ethylene is obtained from an expensive oxygen source providing essentially relatively pure oxygen, i.e., 95+%, along with a substantially lesser but yet significant fraction of one or more diluents, e.g., nitrogen, argon and the like. When added to the process cycle gas, usually in conjunction with a makeup ethylene stream, the oxygen and ethylene mix with a controlled amount of other diluents, other reaction products and contaminants, i.e., carbon dioxide, argon, nitrogen, methane, etc. The precise concentration of the ingredients which can be included is a significant consideration in determining the composition of the reaction gas since the prior art has had no economic way of selectively purging some of these impurities, particularly nitrogen and argon, without also losing large amounts of valuable feed gases, i.e., ethylene. In commercial scale plants excess CO2 -is usually chemically absorbed from the reaction recycle gas by contacting the gas stream with a hot potassium- carbonate solution, stripping out the CO2 with steam, and venting it into the atmosphere with a minimal loss of ethylene. Although such absorption units are expensive and also require significant amounts of energy during operation, they are still economically justified by the reduction in ethylene losses which they provide. In the past the art has controlled the concentration level of diluents such as argon and nitrogen by a less expensive purge type system, i.e., a venting or bleeding step, which unfortunately also results in the loss of a substantial amount of ethylene and therefore a reduced ethylene oxide yield. A significant considetation in forming a suitable reaction gas composition, which typically is made of a majority of diluent ingredients, along with 02 and C2H4, is to form a composition which avoids very high and unstable concentrations of oxygen and/or ethylene. Otherwise, a total combustion of the ethylene content, forming CO2 and water as the reaction products, as well as the danger of an explosion caused by exceeding the flammability limit of the gas composition, can take place. The amount of argon present in the gas is particularly important regarding the flammability issue, since argon is a particularly ineffective component for reducing the flammability of the gas mixture. Thus, a method of selectively monitoring and economically removing certain components, particularly argon, without a substantial loss in reactant gas, particularly ethylene, has been a long felt need in the art. U.S. Patent 3,083,213 is an early teaching on the undesirability of the presence of argon, particularly regarding the flammability factor, in a disclosed ethylene oxide process. U.S. Patent 3,119,837 discloses that methane can be a suitable diluent under certain circumstances in an ethylene oxide process. British Patent 1,321,095 discloses an ethylene oxide process wherein ethylene levels as high as 40-80% by volume are permitted, and in which several diluents are controlled through means of a vent mechanism. In copending case S.N. ¯¯¯¯¯¯¯¯ of Brian Oze & V u 3 1 o Attorney Docket No. 1294, filed concurrently with the present application, the usage of semipermeable membranes to selectively remove CO2 and argon from an ethylene oxide recycle stream is disclosed; the process of Case No. 1294 employs a low purity oxygen feed stream and preferably does not utilize another unit operation to remove CO2 from the system. It is an object of this invention to provide a process for the selective removal of argon from the ethylene-oxygen recycle gas mixture. It is another object of this invention to provide a process for the removal of argon, and accompanying maintenance of the process cycle gas at desired argpn concentrations, without an accompanying substantial loss of ethylene, from the cycle gas. SUMMARY OF THE INVENTION Accordingly, the invention ooarp?rises an improved process for the production of ethylene oxide, ccKtprising reacting ethylene with a subv stantiallypure, e.g., at least 95 mole %, preferably 99+%, oxygen feed stream in the presence of a suitable silverbased catalyst, in a reaction zone under suitable temperatures, e.g., about 200 to 3000C, and super-atmospheric pressures, e.g., about 100 to 400 psia; the reaction occurring in the further presence of a suitable reaction gas mixture, i.e., about 5 to 50 mole % ethylene, 5 to 9 mole % 02' 1 to 25 mole % Ar, 2 to 15 mole % CO2, 0.2 to 1 mole % H20, and 20 to 60 mole % combined CH4 and N2; removing the ethylene oxide product from the reaction effluent gas mixture, e.g. in a scrubbing zone; removing a desired amount of CO2, i.e. the average rate of removal preferably being substantially equal to the average rate at which CO2 is formed during the process, from the reaction gas mixture, preferably by chemical absorption techniques; selectively removing a desired amount of argon, i.e., at an average rate substantially equal to the average rate at which argon enters the feed oxygen stream, e.g., removing about .01 to .5 mole % of the total reaction gas mixture; the removal occurring by passing a suitable amount, e.g., about e 2 25%, preferably 2 to 5%, of the reaction gas mixture through a suitable semipermeable membrane unit, i.e., a membrane unit maintained at a pressure differential of about 10 to 400 psi, preferably about 100 to 250 psi; replenishing the depleted reactant gas mixture with fresh feed, i.e., 2 and C2H4, and repeating the process cycle. DESCRIPTION OF THE DRAWINGS Figure 1 sets forth a brief outline of the preferred process of the invention described. DETAILED DESCRIPTION OF THE INVENTION Ethylene oxide today is produced commercially through the silver catalyzed, vapor phase incomplete oxidation of ethylene by molecular oxygen. Typically, the product ethylene oxide generally constitutes but a relatively small percentage of the total effluent stream leaving the oxidation reaction zone, e.g., about 1 to 3 mole %. The remainder of the reactor effluent comprises several diluents and reaction byproducts; the diluents functioning to negate the possibility of explosions and unwanted combustibility levels being attained during the reaction. If the so-called flammability limit, i.e., at which point the complete and rapid oxidation of ethylene to CO2 and water can occur, is exceeded, the possibility of a serious explosion becomes a very real factor. Naturally, it is desired to operate under conditions which will maximize the conversion of ethylene to ethylene oxide, yet avoid safety problems while maintaining an industrially acceptable reaction rate. In an effort to find such an optimum environment, gases such as nitrogen and methane are intentionally introduced and along with the reaction byproduct carbon dioxide, and argon, which enters as an impurity in the oxygen feed, are maintained at predetermined concentrations in the recycle reaction gas. The goal of such composition setting is to find an optimum mixture which permits one to safely react maximum concentrations of oxygen and ethylene to form ethylene oxide, thus increasing the selectivity of the ethylene present to ethylene oxide. Some of the diluents present in the recycle gas owe their origin to a gradual accumulation of impurities which are present in the reactant gas feed streams. This is certainly the case with argon1 which enters the system as the major impurity present in the oxygen feed stream. The art has been unable to find a selective manner of removing the excess argon which builds up in the system, other than by simply purging a predetermined amount of the recycle gas mixture through a bleed stream which is then discarded. Such a purge gas, unfortunately, also contains a high ethylene concentration and results in a substantial ethylene loss, e.g., from about 0.1 to 5.0 mole % of the mixture, the magnitude of which depends on the argon content in the oxygen feed and the recycle gas stream. Surprisingly, we have discovered that the addition of a suitable semipermeable membrane unit, e.g., either a single unit or a multi-stage membrane configuration, with a typical separator unit installed in a pressure vessel in a manner analogous to a shell and tube heat exchanger, can efficiently and selectively extract the argon from the remaining recycle mixture. The feed gas, i.e., a desired amount of t-he recycle gas stream, is first fed into the shell side of the separator. Due to the presence of a significant pressure differential, e.g., from about 20 to 400 psi and preferably from about 100 to 250 psi between the outer and inner sides of the membrane tube of fibre, the argon component desired to be separated more easily permeates through the membrane film as the gas stream traverses the length of the bundle. The resultant selective separation yields a permeate stream with a significantly higher, e.g., from about a 1.5 to 1 to a 50 to 1 argon to ethylene mole ratio on the inner side of the membrane tube or fibre than in the non-permeate, ethylene-rich shell side stream. The relative rate of permeation of each component present in the gas mixture is, in general, a function of the individual component's partial pressure differential across the fibre wall, as well as the onçonent's solubility and diffusivity in the fibre. A preferred semipermeable membrane for use in the process is that sold under the-"'V trade name "PRISM" by Monsanto Company, St. Louis, Missouri, but a wide variety of other such membrane units, as will be apparent to one skilled in the membrane art, are within the scope of the invention. The process of the invention is of the type in which substantially pure molecular oxygen, in contrast to less pure oxygen or air, is employed as the makeup feed stock to replenish the oxygen consumed in the reaction. Purified oxygen having an oxygen content of at least about 95 mole % is introduced as a makeup stream into the system, the oxygen preferably being present in purity ranging from about 99.0 to 99.9 mole %. It is also desirable to operate in the range of high ethylene concentrations, in order to achieve a high ethylene selectivity to ethylene oxide, as this is clearly essential for commercial operation, and thus ethylene concentrations as high as about 40 to 50 mole % can be present in the recycle gas mixture. It is preferred, and almost essential for effective operation-that the argon present in the oxygen makeup feed not exceed the range of - about 0.1 to 5.0 mole %, typically about 0.5 mole % of the oxygen feed. The gas mixture comprising the recycle reaction gas stream, in addition to the feed gases and the different impurities, also contains significant amounts of certain reaction products, e.g., the CO2 formed as a major byproduct which has not been removed, water, and a small amount of unremoved ethylene oxide. Figure 1 sets forth a simplified outline of the preferred embodiment of the process. The system comprises a reactor unit 2 containing a suitable silver metal-based catalyst known to those in the art, e.g., such as that disclosed in U.S. Patent 3,725,307, as well as many others, and through which an ethylene and oxygen containing mixture, entering through line 4 is passed, with fresh makeup ethylene and oxygen having been introduced earlier into line 4. A reactor effluent stream comprising ethylene oxide, unreacted feed components, various diluents wh reaction byproducts is withdrawn from reactor unit 2 through line 6 and, after preferably being cooled in heat exchanger 8, preferably by warming the incoming reactor feed mixture in line 4, passes into a scrubbing unit (or another suitable separation unit) 10 wherein the gas mixture is scrubbed by contacting with an aqueous stream or another suitable ethylene oxide scrubbing agent entering through line 12 and eventually leaving the unit containing the absorbed ethylene oxide through line 14, from which stream the ethylene oxide is eventually extracted therefrom as product. The ethylene oxide-free effluent passes out of the scrubber through line 16 and passes through a mist separator 18 which removes any entrained liquid present. The scrubbed gas from separator 18 exits through line 20, and enters a compressor unit 22, where it is raised to a desired pressure, e.g., about 240 to 340 psia. The now pressurized gas stream passes through line 24 typically comprising about 5-15 mole t argon and from 5 to 15 mole % CO2 whereupon the recycle stream is divided order to remove the excess CO2 and excess argon, with typically about 10 to 20% passing through line 26 into CO2 removal unit 28, about 0.5 to 25% passing through line 30 into the semipermeable membrane unit 32, while the remaining gas stream passes through bypass line 34 leading back towards the reactor. In membrane unit 32, the preferred design of which has been described above, a small, argon-enriched and ethylene-lean permeate stream (its argon content comprising about .001 to 0.1 mole %, preferably about .018 of the total reaction gas mixture) is separated from the entering gas mixture and suitably disposed of through line 33, such as by being fed to the incinerator or the like, while the non-permeate stream, preferably only slightly reduced in argon concentration, passes out of the membrane unit through line 36. Concurrently, the fraction of the recycle gas mixture which passes into C02 removal unit 28 is preferably treated for removal of C02 in a large commercial plant by conventional low ethylene loss means, e.g., a hot carbonate scrubber system, or the like, with the extracted CO2-rich stream preferably vented through line 29, or otherwise suitably disposed of. The treated, C02-reduced frac- tion exits removal unit 28 through line 38 and preferably reunites with bypassed stream in line 34 and the exit gas from membrane unit 32 (line 36) to form the resulting cycle gas feed mixture present in line 4. About 5-258 of the CO2 present is typically removed from the system in this manner. In the broadest embodiment of the invention the removal of argon, or CO2, can take place at any point in the process cycle, starting from the removal of ethylene oxide product from the gas stream until prior to the addition of an ethylene makeup stream, although it is preferred to do so in the manner as earlier described. Other suitable locations for the argon membrane removal unit of particular note are on the line containing the gas stream 38 exiting the CO2 removal unit, and also to recycle the non-permeate effluent from the membrane unit back to the compressor suction (line 20). The treated recycle gas mixture is then preferably replenished by both ethylene and oxygen makeup streams 40 and 42, respectively; there being a great amount of discretion regarding the precise point of introduction, and such location forming no part of the invention. The stream preferably again passes through heat exchanger 8 and enters the reactor, the process is continued indefinitely. The controlled oxidation reaction can be carried out at temperatures ranging from 150-4504C, preferably in the range from about 200-300 C. Suitable pressures which can be employed range from about 100 psia to about 400 psia, although higher pressures can be used if so desired. It is of course understood that a wide variety of other embodiments than the one disclosed are suitable for use in the invention.

Claims: CLAIMS 1. A process for the production of ethylene oxide comprising: reacting ethylene with oxygen to form ethylene oxide in a reaction zone in the presence of a suitable silver-based catalyst, under suitable temperatures and superatmospheric pressures; the reaction occurring in the further presence of a suitable reaction gas mixture containing a C02 and argon component; removing the formed ethylene oxide from the reaction effluent gas mixture; selectively removing a suitable amount of argon by passing a suitable amount of the reaction gas mixture through a suitable semipermeable membrane unit; and replenishing the depleted reactant gases. 2. The process as claimed in claim 1 wherein the oxygen supplied to the process is a substantially pure 02 stream containing at least 95 mole % 02. 3. The process as claimed in claim 1 wherein the oxygen is supplied to the process as at least about 99 mole % 02. 4. A process as claimed in claim 1, claim 2 or claim 3 wherein a suitable amount of C02 is selectively removed from the reaction gas mixture. 5. A process as claimed in claim 4 wherein the CO2 is removed from the reaction gas mixture by chemical absorption. 6. A process as claimed in claim 4 or claim 5 wherein the average rate at which CO2 is removed from the reaction gas is substantially equal to the average rate at which CO2 is formed during the process. 7. A process as claimed in any one of claims 1 to 6 wherein the argon component present in the reaction gas mixture is substantially supplied to the reaction gas as a diluent in the feed 2 gas stream. 8. A process as claimed in any one of claims 1 to 7 wherein the reaction zone is maintained at about 200-3000C and 100-400 psia. 9. A process as claimed in any one of claims 1 to 8 wherein the reaction gas mixture comprises about 5-50 mole % ethylene, 5 to 9% 021 1 to 25% argon 2 to 15% C02, 0.2 to 1% water and 20 to 60% combined methane and nitrogen. 10. A process as claimed in any one of claims 1 to 9 wherein the ethylene oxide product is removed from the effluent gas mixture in a suitable stripping zone. 11. A process as claimed in any one of claims 1 to 10 wherein the average rate at which argon is removed from the gas mixture is substantially equal to the average rate at which it enters the reaction gas mixture in the feed oxygen stream. 12. A process as claimed in any one of claims 1 to 11 wherein the amount of argon removed from the reaction gas mixture is equal to about 0.001 to 0.1 mole % of the total reaction gas mixture. 13. A process as claimed in any one of claims 1 to 12 wherein about 0.5 to 25 mole % of the reaction gas mixture is passed through the membrane separation unit. 14. A process as claimed in any one of claims 1 to 13 wherein the membrane unit is maintained at a pressure differential of about 20 to 400 psi. 15. A process as claimed in any one of claims 1 to 14 wherein the depleted reactant gases are suitably replenished with fresh feed. 16. A process as claimed in claim 15 where the replenished reactants are ethylene and oxygen. 17. A process as claimed in any one of claims 1 to 16 wherein the process cycle is continually repeated. 18. A process as claimed in any one of claims 1 to 17 wherein the ratio of argon t6 ethylene in the argon-rich permeate stream compared to - the ethylene-rich, non-permeate stream ranges from about 1.5 to 1 to 50 to 1. 19. A process as claimed in any one of claims 1 to 18 wherein the reaction - of ethylene with oxygen to form ethylene oxide occurs in the vapour phase.

Inventors: OZERO, BRIAN J.
Applicants: SCIENTIFIC DESIGN COMPANY INC.
Application year: 1986
Main classification: C07D301
IPC codes: B01J23, C07D303, C07B61, C07D301