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

The invention generally relates to processes for reducing fouling in amine systems and to equipment useful in such processes. Such amine systems are useful for removing one or more acidic gases such as CO.sub.2 or H.sub.2S from olefin containing hydrocarbon streams. The invention generally relates to minimizing residence time of foulant and foulant precursors at the relatively high temperature found in the amine regenerator and/or to purging the foulant and foulant precursors from the regenerator system. This is accomplished by operating the regenerator column as a stripper (no reflux) and re-routing reflux liquid containing foulant or foulant precursors to a processing location that is less prone to fouling or, optionally, by replacing the reflux liquid with fresh make-up amine or water.

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 tank end 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.

Disclosed is an improved process for regenerating solvent used to remove contaminants from a fluid stream. Said process comprises a solvent regeneration system (10) comprising a rich/lean solvent stripper column (29), reboiler (50), condenser (36), and reflux receiver (38) wherein the improvement is the location 46 of the condensed stripper gas return from the reflux receiver.

Fractionation systems utilizing a single rectifying column with a stripping column housed in the same vessel and having a uniform diameter are described. Methods of separating feed streams using the fractionation systems are also described.

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.

The present invention provides a gas pressurized separation system to strip a product gas from a liquid stream and yield a high pressure gaseous effluent containing the product gas. The system comprises a gas pressurized stripping apparatus, such as a column, with at least one first inlet allowing flow of one or more liquid streams in a first direction and at least one second inlet allowing flow of one or more high pressure gas streams in a second direction, to strip the product gas into the high pressure gas stream and yield through at least one outlet a high pressure gaseous effluent containing the product gas; and two or more heat supplying apparatuses provided at different locations along the column. Processes for separating a product gas from a gaseous mixture to yield a high pressure gaseous effluent containing the product gas, utilize the gas pressurized separation system described above.

Systems and processes for reducing the energy requirements of an ammonia recovery stripper in a chilled ammonia-based CO.sub.2 removal system. The systems and processes include a nanofiltration or reverse osmosis unit for physically separating the washed liquid from a wash vessel configured to receive an ammonia slip feed stream from the main absorber of the chilled ammonia-based CO.sub.2 removal system and provide first and second feed streams. Relative to the washed liquid from the wash vessel, the first feed stream has a decreased ammonia molarity whereas the second feed stream has an increased ammonia molarity. The second feed stream is then fed to the ammonia recovery stripper, which reduces steam consumption. The reduced steam consumption translates to significant energy savings, among numerous other advantages. Additionally, the systems and process provide a reduction of equipment sizes related to the stripper unit as may be desired in some applications.

CO.sub.2 absorber includes a CO.sub.2 absorbing section in which a CO.sub.2-containing flue gas and a CO.sub.2 absorbent are brought into contact with each other to remove CO.sub.2, and an aqueous cleaning section in which a decarbonated flue gas and rinsing water are brought into contact with each other to remove an accompanying substance. A lean solution is re-used in the absorber. The CO.sub.2 recovery device includes a degassing basin which is interposed in a rich solution supply line that supplies the rich solution from the CO.sub.2 absorber to the absorbent regenerator, and which includes a retaining section configured to remove oxygen in the rich solution.

A process for the preparation of glycol ethers by providing a diethylene glycol ether column bottoms mixture comprising triethylene glycol ether, tetraethylene glycol ether, and glycol ether catalyst; separating, in a stripping column, the column bottom mixture into a triethylene glycol ether vapor overhead and a liquid bottoms; and separating, in an evaporator, the liquid bottoms into a residue containing about 80% to about 90% tetraethylene glycol ether and an evaporator overhead comprising at least about 60% tetraethylene glycol ether.