Processes, systems, and apparatus are provided for producing a compressed process gas comprising light olefin such as ethylene. The process utilizes a pyrolysis reactor to produce the process gas. A power generator utilizes a turbine operated based on an Allam cycle to produce shaft power for operating one or more compressors involved in processing of the process gas while producing a reduced or minimized amount of CO.sub.2 that is released as a low-pressure gas phase product. Examples of using the shaft power for processing of the process gas can include compressing the process gas a process gas compressor powered by the produced shaft power and cooling the process gas using a refrigeration compressor powered by the produced shaft power.

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (C.sub.2H.sub.6, C.sub.2H.sub.4, O.sub.2) to a first reactor system to produce a first effluent stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactor system is characterized by a first reactor system operating temperature of 270° C.-320° C.; wherein the first reactor system comprises oxidative dehydrogenation (ODH) stage(s); (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); wherein ethylene is not separated from recycle stream and/or first effluent stream; (d) recycling at least a portion of recycle stream to the first reactor system, and a optionally portion of recycle stream to the second reactor.

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (C.sub.2H.sub.6, C.sub.2H.sub.4, O.sub.2) to a first reactor system to produce a first effluent stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactor system is characterized by a first reactor system operating temperature of 270° C.-320° C.; wherein the first reactor system comprises oxidative dehydrogenation (ODH) stage(s); (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); wherein ethylene is not separated from recycle stream and/or first effluent stream; (d) recycling at least a portion of recycle stream to the first reactor system, and a optionally portion of recycle stream to the second reactor.

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (C.sub.2H.sub.6, C.sub.2H.sub.4, O.sub.2) to a first reactor to produce a first effluent stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactant mixture is characterized by a molar ratio of ethylene to ethane of ≥1.3; (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); wherein ethylene is not separated from recycle stream and/or first effluent stream; and (d) recycling at least a portion of recycle stream to the first reactor, and a portion of recycle stream to the second reactor.

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (C.sub.2H.sub.6, C.sub.2H.sub.4, O.sub.2) to a first reactor to produce a first effluent stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactant mixture is characterized by a molar ratio of ethylene to ethane of ≥1.3; (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (C.sub.2H.sub.4, C.sub.2H.sub.6, O.sub.2); wherein ethylene is not separated from recycle stream and/or first effluent stream; and (d) recycling at least a portion of recycle stream to the first reactor, and a portion of recycle stream to the second reactor.

In one aspect, the present invention encompasses integrated processes for the conversion of epoxides to acrylic acid derivatives and polyesters. In certain embodiments, the methods of the present invention comprise the steps of: providing a feedstock stream comprising an epoxide and carbon monoxide; contacting the feedstock stream with a metal carbonyl in a first reaction zone to effect conversion of at least a portion of the provided epoxide to a beta lactone; directing the effluent from the first reaction zone to a second reaction zone where the beta lactone is subjected to conditions that convert it to a compound selected from the group consisting of: an alpha beta unsaturated acid, an alpha beta unsaturated ester, an alpha beta unsaturated amide, and an optionally substituted polypropiolactone polymer; and isolating a final product comprising the alpha-beta unsaturated carboxylic acid, the alpha-beta unsaturated ester, the alpha-beta unsaturated amide or the polypropiolactone.

In one aspect, the present invention encompasses integrated processes for the conversion of epoxides to acrylic acid derivatives and polyesters. In certain embodiments, the methods of the present invention comprise the steps of: providing a feedstock stream comprising an epoxide and carbon monoxide; contacting the feedstock stream with a metal carbonyl in a first reaction zone to effect conversion of at least a portion of the provided epoxide to a beta lactone; directing the effluent from the first reaction zone to a second reaction zone where the beta lactone is subjected to conditions that convert it to a compound selected from the group consisting of: an alpha beta unsaturated acid, an alpha beta unsaturated ester, an alpha beta unsaturated amide, and an optionally substituted polypropiolactone polymer; and isolating a final product comprising the alpha-beta unsaturated carboxylic acid, the alpha-beta unsaturated ester, the alpha-beta unsaturated amide or the polypropiolactone.

Systems and methods for producing ethylene oxide (EO) are disclosed. Ethylene oxide is produced by direct oxidizing ethylene with oxygen in a reactor. The effluent from the reactor is processed to produce (a) a product stream comprising water and ethylene oxide, (b) a reabsorber overhead stream comprising ethylene, methane, argon, and carbon dioxide, and (c) a carbonate flash gas stream comprising carbon dioxide, ethylene, methane, and water. The reabsorber overhead stream and the carbonate flash gas stream are combined to form a reclaim gas stream. The reclaimed gas stream is separated in a membrane separation unit to remove carbon dioxide and argon, forming a recycle stream comprising primarily ethylene and methane, collectively.

Systems and methods for producing ethylene oxide (EO) are disclosed. Ethylene oxide is produced by direct oxidizing ethylene with oxygen in a reactor. The effluent from the reactor is processed to produce (a) a product stream comprising water and ethylene oxide, (b) a reabsorber overhead stream comprising ethylene, methane, argon, and carbon dioxide, and (c) a carbonate flash gas stream comprising carbon dioxide, ethylene, methane, and water. The reabsorber overhead stream and the carbonate flash gas stream are combined to form a reclaim gas stream. The reclaimed gas stream is separated in a membrane separation unit to remove carbon dioxide and argon, forming a recycle stream comprising primarily ethylene and methane, collectively.

Disclosed are gas-phase ODH and OCP processes for converting alkanes (e.g., C.sub.2H.sub.6 and C.sub.3H.sub.8) to alkenes (e.g., C.sub.2H.sub.4 and C.sub.3H.sub.6) or oxygenates (e.g., methanol, ethanol, isopropanol, or propylene oxide) or converting alkenes (e.g., ethylene and propene) and oxygenates (e.g., methanol, ethanol, isopropanol or propylene oxide) to longer carbon-chain alkenes or longer carbon-chain alkanes with or without solid catalysts.