A deaerator includes a vessel having a chamber defined by an outer wall; and a tray module detachably connected to the vessel, the tray module having a plurality of deaerator trays which are connected to one another in a spaced relationship to form a stack which is suspended within the chamber.

An improved system for separating gas from a process stream by providing a stripping unit at the overhead stream of a fractionation column to selectively and effectively remove the gas using a stripping fluid without providing a dedicated light-ends separations unit. The stripper unit may be connected to the reflux drum at the overhead stream. The system for separating gas further achieves greater thermodynamic efficiency by means of a split column design using mechanical vapor recompression with the reboiler and condenser integrated in a falling-film evaporator- or thermosiphon-type vapo-condenser.

A gas condensing device may be configured to condense regeneration gas and separate target gas from condensate. The gas condensing device may include: a housing; a condenser mounted in an upper portion of the housing and configured to condense the regeneration gas; and a reflux apparatus mounted in the housing below the condenser and configured to temporarily store the condensate and discharge evaporation gas evaporated from the condensate back to the condenser.

An absorbent regenerator includes: a rich solution supply line; a lean solution supply line; a lean-rich solution heat exchanger that is provided at an intersection of the lean solution supply line and the rich solution supply line; a branch portion that branches some of the rich solution at a downstream side of the lean-rich solution heat exchanger on the rich solution supply line; and a first mixing portion that mixes the some of the rich solution branched at the branch portion with a semi-lean solution, wherein a front end of a branch line through which the some of the branched rich solution is supplied is connected to a solution storage portion of the semi-lean solution which is located at an upper stage side of the absorbent regenerator divided into parts, and the some of the branched rich solution is mixed with the semi-lean solution.

A CO.sub.2 recovery device includes: a CO.sub.2 absorption tower in which CO.sub.2 included in an exhaust gas is absorbed by a CO.sub.2 absorption liquid; and a CO.sub.2 absorption liquid regeneration tower that heats and regenerates the CO.sub.2 absorption liquid that has absorbed CO.sub.2. The CO.sub.2 absorption liquid regeneration tower includes: a main body part in which the CO.sub.2 absorption liquid is temporarily stored; a boot part provided downward from a mirror surface part of the main body part, having a relatively smaller capacity than the main body part; a flowmeter provided to the boot part, and measuring the liquid surface level of the CO.sub.2 absorption liquid that changes between the main body part and the boot part; and a control device controlling the liquid surface level of the CO.sub.2 absorption liquid between the main body part and the boot part on the basis of the measurement result of the flowmeter.

Systems, apparatuses, and methods for conditioning fluid, for example, to reduce the concentration of a contaminant in a fluid are provided. In one embodiment, the method comprises: introducing a contaminated fluid and a first stripping gas into a first vessel; contacting the contaminated fluid with the first stripping gas to reduce the concentration of a contaminant in the contaminated fluid; transferring the contaminated fluid into a second vessel; introducing a second stripping gas into the second vessel; and contacting the contaminated fluid with the second stripping gas to further reduce the concentration of the contaminant in the contaminated fluid.

Systems and methods for enhanced separation of H2S and NH3 in an H2S stripper using carbon dioxide and/or an inert gas.

The present invention relates to an oil refining equipment comprising a stripping column with packing and the column has a height to diameter ratio from 0.1 to 10, from 0.5 to 5, from 1 to 4.9, from 1.4 to 4.5, from 1.6 to 2.8. It is used for degrading, decomposing or breaking down oxidation products of triglycerides, diglycerides, monoglycerides and/or fatty acids. A process for refining edible oils is described as well.

A process for producing synthesis gas, the process comprising the steps of a) reforming a hydrocarbon feed in a reforming section thereby obtaining a synthesis gas comprising CH4, CO, CO2, H2 and H2O and impurities comprising ammonia; b) shifting the synthesis gas in a shift section comprising one or more shift steps in series to a shifted synthesis gas; c) separating from the shifted synthesis gas a process condensate originating from cooling and optionally washing of the shifted synthesis gas; d) passing a part of the process condensate to a condensate steam stripper, wherein dissolved shift byproducts comprising ammonia, methanol and amines formed during shifting the synthesis gas are stripped out of the process condensate using steam resulting in a stripper steam stream, e) adding the stripper steam stream from the process condensate steam stripper to the hydrocarbon feed and/or to the synthesis gas downstream the reforming section, up-stream the last shift step, wherein the remaining part of the process condensate is purged.

Methods of crude oil stabilization may include separating crude oil in a bulk separator into a first light hydrocarbon stream, a first water stream, and a first bottoms stream; separating the first bottoms stream in an intermediate pressure separator into a second light hydrocarbon stream, a second water stream, and a second bottoms stream; separating the second bottoms stream in a separator into a third light hydrocarbon stream, a third water stream, and a third bottoms stream; introducing a stripping gas stream comprising methane into the separator; storing the third bottoms stream in a vessel comprising an outlet for a fourth light hydrocarbon stream; treating at least a portion of the first, second, third, and fourth light hydrocarbon streams in a vapor treatment process to form a final light hydrocarbon stream; and recycling at least a portion of the final light hydrocarbon stream to the separator.