Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, H.sub.2SO.sub.4 alkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit.

Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, H.sub.2SO.sub.4 alkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit.

A process is presented for the production of butadienes. The process includes the recovery of a crude butadiene stream using adsorption separation and removes the need to compress the effluent stream from the oxidative dehydrogenation process effluent stream. The process includes an adsorption step to remove C4 compounds from the oxidative effluent stream, a desorption step to recover the adsorbed C4 compounds and a regeneration step to regenerate the adsorbent for continued use in the separation process.

A process for removing light components from an ethylene stream may include providing a dried ethylene stream containing ethylene, ethane, CO, CO.sub.2, H.sub.2, CH.sub.4, and C.sub.3+ hydrocarbons. The process may include sending the dried ethylene stream to a stripper to produce an overhead stream containing ethylene, CO, H.sub.2 and CH.sub.4, and a bottom stream containing ethylene, ethane, CO.sub.2, and C.sub.3+ hydrocarbons. The gaseous phase on top of the stripper may be condensed in a heat exchanger cooled by a refrigerant stream to get a first gaseous phase and a first liquid phase. The first gaseous phase may be condensed in a heat exchanger cooled by liquid ethane or liquid ethylene to get a second gaseous phase containing ethylene CO, H.sub.2 and CH.sub.4 and a second liquid phase. The first and second liquid phases may be the reflux of the stripper.

A process for removing light components from an ethylene stream may include providing a dried ethylene stream containing ethylene, ethane, CO, CO.sub.2, H.sub.2, CH.sub.4, and C.sub.3+ hydrocarbons. The process may include sending the dried ethylene stream to a stripper to produce an overhead stream containing ethylene, CO, H.sub.2 and CH.sub.4, and a bottom stream containing ethylene, ethane, CO.sub.2, and C.sub.3+ hydrocarbons. The gaseous phase on top of the stripper may be condensed in a heat exchanger cooled by a refrigerant stream to get a first gaseous phase and a first liquid phase. The first gaseous phase may be condensed in a heat exchanger cooled by liquid ethane or liquid ethylene to get a second gaseous phase containing ethylene CO, H.sub.2 and CH.sub.4 and a second liquid phase. The first and second liquid phases may be the reflux of the stripper.

Disclosed in certain embodiments are sorbents for capturing heavy hydrocarbons via thermal swing adsorption processes.

Disclosed in certain embodiments are sorbents for capturing heavy hydrocarbons via thermal swing adsorption processes.

Disclosed is a process for regenerating a hybrid solvent used to remove contaminants from a fluid stream and to provide an improved yield of purified fluid. Said process comprises at least one purification unit (12) and at least one regeneration unit (40) wherein condensed water 62 from the regeneration unit is recycled back into the purification unit and none of the condensed water is reintroduced into the regeneration unit.

Disclosed is a process for regenerating a hybrid solvent used to remove contaminants from a fluid stream and to provide an improved yield of purified fluid. Said process comprises at least one purification unit (12) and at least one regeneration unit (40) wherein condensed water 62 from the regeneration unit is recycled back into the purification unit and none of the condensed water is reintroduced into the regeneration unit.

Treatment of hydrocarbon streams, and in one non-limiting embodiment refinery distillates, with high pH aqueous reducing agents, such as borohydride, results in reduction of the sulfur compounds such as disulfides, mercaptans and thioethers that are present to give easily removed sulfides. The treatment converts the original sulfur compounds into hydrogen sulfide or low molecular weight mercaptans that can be extracted from the distillate with caustic solutions, hydrogen sulfide or mercaptan scavengers, solid absorbents such as clay or activated carbon or liquid absorbents such as amine-aldehyde condensates and/or aqueous aldehydes.