The invention relates to a gas scrubbing process and a corresponding plant for removal of acidic gas constituents from crude synthesis gas which make it possible by treatment of shifted and of unshifted crude synthesis gas in the gas scrubbing process and by combination of the thus-obtained partial product streams to produce a plurality of gas products having different compositions. In addition, the invention ensures that the flash gases obtained during decompression of the laden scrubbing medium are utilized materially and/or energetically in advantageous fashion.

The invention relates to a process for removal of unwanted, in particular acidic gas constituents, for example carbon dioxide and hydrogen sulfide, from a crude synthesis gas by gas scrubbing with a scrubbing medium. According to the invention the flash gases obtained during the decompression of the laden scrubbing medium are supplied to a recompressor in order to recycle these to the crude synthesis gas and thus utilize them materially after the recompression. Alternatively or in addition the flash gases may also be supplied to a decompression turbine to recover refrigeration and mechanical work. If the recompressor and/or the decompression turbine are/is designed to have multiple stages, the flash gases obtained at different pressure levels are preferably supplied to a corresponding pressure level of the recompressor and/or of the decompression turbine.

A plant for removing CO.sub.2 from a fluid stream via an aqueous absorption medium contains a) a first absorption zone for treating the fluid stream with a partially regenerated absorption medium, b) a second absorption zone for treating the treated fluid stream with a regenerated absorption medium, c) a first flash vessel for depressurizing the loaded absorption medium, d) a second flash vessel for depressurizing the sub-partially regenerated absorption medium, e) a stripper for thermally regenerating the partially regenerated absorption medium, f) a conduit for feeding a substream of the partially regenerated absorption medium into the first absorption zone and a conduit for feeding a further substream of the partially regenerated absorption medium into a stripper, g) a conduit for recirculating the regenerated absorption medium to the second absorption zone, and h) a jet pump for compressing the water vapor-comprising, second CO.sub.2-comprising gas stream.

Embodiments of point-of-use (POU) abatement device and methods of abating a plurality of gas streams from a corresponding plurality of processing chambers are provided herein. In some embodiments, a compact POU abatement device includes a plurality of inlets respectively coupled to a plurality of process chambers in which each of the process chambers gas streams is isolated from the other gas streams. In some embodiments, the compact POU abatement device can include a plurality of oxidation devices and a corresponding plurality of wet scrubber columns each directly coupled to ones of the plurality of inlets to receive a gas stream from a corresponding process chamber.

A gas processing system is described herein. The gas processing system includes a number of co-current contacting systems configured to contact a sour feed gas stream including an acid gas with a solvent stream to produce a partially-sweetened gas stream and a rich solvent stream including an absorbed acid gas. At least one of the co-current contacting systems is configured to send the rich solvent stream to a regenerator. The regenerator is configured to remove the absorbed acid gas from the rich solvent stream to produce a lean solvent stream. The gas processing system also includes a solvent treater configured to treat at least a portion of the lean solvent stream to produce an enhanced solvent stream, and a final co-current contacting system configured to contact the partially-sweetened gas stream with the enhanced solvent stream to produce a partially-loaded solvent stream and a final gas stream.

Organic sulfur compounds contained in refinery off gas streams having either high ort low concentrations of olefins are converted to hydrogen sulfides which can be then be removed using conventional amine treating systems. The process uses a catalytic reactor with or without a hydrotreater depending on the olefin concentration of the off gas stream. The catalytic reactor operates in a hydrogenation mode or an oxidation mode to convert a majority of organic sulfur compounds into hydrogen sulfides.

Processes and systems for the production of ethylbenzene using a dilute ethylene feed and subsequent recovery of ethane in the alkylation vent gas.

A flare gas recovery system includes a primary gas sweetening unit; and a liquid-driven ejector in continuous fluid communication with the primary gas sweetening unit. The ejector includes an inlet configured to receive a motive fluid including a regenerable amine solvent in a rich state from the primary gas sweetening unit; a gas inlet configured to receive a suction fluid including a gas; and a fluid outlet configured to either directly or indirectly discharge to the primary gas sweetening unit a two-phase fluid including a mixture of the suction fluid and the amine solvent in a rich state.

Controlling aerosol production during absorption in ammonia-based desulfurization. The absorption reaction temperature, the oxygen content and water content of the process gas may be controlled, and an absorption circulating liquid containing ammonium sulfite may be used for removing sulfur dioxide in flue gas, so as to control aerosol production during absorption in the ammonia-based desulfurization

The present invention relates to an improved process and system for purifying a gas, preferably an energy gas, containing aromatic compounds and isolating a fraction of aromatic compounds from said gas. In the process according to the invention, the gas is contacted with a washing liquid in step (a), at a temperature of 15-250° C., to obtain a purified gas, which is depleted in aromatic compounds, and a spent washing liquid wherein the aromatic compounds are dissolved. The spent washing liquid is stripped in step (b) with a stripping gas comprising at least 50 vol. % steam, to obtain a stripped washing liquid which is advantageously reused in step (a) and a loaded stripping gas comprising the aromatic compounds. The aromatic compounds are separated from the loaded stripping gas in step (c) by condensation of the steam and/or the aromatic compounds comprised in the loaded stripping gas to obtain an immiscible composition and isolating the aromatic compounds therefrom. The cleared stripping gas which is advantageously reused in step (b).