Abstract: The present invention is directed to a process for the removal of aromatic hydrocarbons from a lean acid gas containing less than 20 mol.

Abstract: The present invention relates to a liquid-gas contacting unit comprising a column, at least a lower packed bed and a higher packed bed positioned higher than the lower packed bed inside the column, a gas-tight liquid collecting and redistributing device disposed between the lower and the higher packed bed inside the column and an external pipe outside the column, the external pipe comprising an inlet end, an outlet end and a peripheral wall between the inlet end and the outlet end; the inlet end being positioned between the lower pack bed and the gas-tight liquid collecting and redistributing device and the outlet end being positioned between the higher pack bed and the gas-tight liquid collecting and redistributing device. The present invention also relates to a method for improving the efficiency of a liquid-gas contacting unit.

Abstract: A process for the removal of hydrogen sulfide and sulfur recovery from a H2S-containing gas stream by catalytic direct oxidation and Claus reaction through two or more serially connected catalytic reactors, wherein a specific control of the oxygen supplement is operated. The control and improvement of the process is obtained by complementing, in each major step of the process, the H2S-containing gas stream by a suitable flow of oxygen, namely before the H2S-containing gas stream enters the Claus furnace, in the first reactor of the process and in the last reactor of the process. Especially in application in a SubDewPoint sulfur recovery process the H2S/SO2 ratio is kept constant also during switch-over of the reactors R1 and R by adding the last auxiliary oxygen containing gas directly upstream the last reactor R so that the H2S/SO2 ratio can follow the signal of the ADA within a few seconds.

Abstract: The present invention relates to a gas-redirecting device presenting an upper plane and a plurality of gas-redirecting tubes comprising an inlet end and an outlet end. For each gas-redirecting tube, the orthogonal projections of the inlet end and the outlet end onto the upper plane have an over-lapping area of at most 50% of the total area of the upper plane covered by the orthogonal projections. Also provided is a liquid-gas contacting column comprising a gas-redirecting device, a floating support comprising a liquid-gas contacting column, at least two packed beds and a method for improving the efficiency of a liquid-gas contacting column which is based on redirecting the gas from a wetted zone of a lower packed bed to a wetted zone of the higher packed bed.

Abstract: The present invention relates to a column for exchanging material and, if appropriate, heat between a gas and a liquid. The column comprises at least one collector tray 1 and a liquid distribution system 5, 6 arranged between two packed beds 7, and gas and liquid separation means 8. The present invention proposes arranging gas and liquid separation means 8 between the collector tray 4 and the liquid distribution means 5, 6.

Abstract: The present invention relates to a column for exchanging heat and/or material between a gas and a liquid. The column comprises at least one collector tray (1), at least one packed bed, and mixing means for a gas flow (7, 8). According to the invention, the mixing means for a gas flow are arranged below the collector tray (1) and above the packing.

Abstract: The present invention is directed to a process for the removal of aromatic hydrocarbons from a lean acid gas containing less than 20 mol.

Abstract: The invention concerns a flexible process for purifying a solvent which inhibits the formation of hydrates during gas processing, in particular monoethylene glycol (MEG), said solvent having a boiling point which is higher than that of water and, at least at one point in time, being mixed with water and salts, the process operating in a different manner with the same facility as a function of the quantity of salts in the MEG to be treated. The process operates in accordance with a phase known as reclaiming (separation of salts under vacuum followed by vacuum distillation) when the salts content exceeds the precipitation threshold and if not, the process operates in a regeneration phase (absence of separation of salts and no operation under vacuum). Advantageously, the change is made under the control of means for testing the salts.

Abstract: A process for the removal of hydrogen sulfide and sulfur recovery from a H2S-containing gas stream by catalytic direct oxidation and Claus reaction through two or more serially connected catalytic reactors, wherein a specific control of the oxygen supplement is operated. The control and improvement of the process is obtained by complementing, in each major step of the process, the H2S-containing gas stream by a suitable flow of oxygen, namely before the H2S-containing gas stream enters the Claus furnace, in the first reactor of the process and in the last reactor of the process. Especially in application in a SubDewPoint sulfur recovery process the H2S/SO2 ratio is kept constant also during switch-over of the reactors R1 and R by adding the last auxiliary oxygen containing gas directly upstream the last reactor R so that the H2S/SO2 ratio can follow the signal of the ADA within a few seconds.

Abstract: A process for removing sulfur from a gas containing sulfur compounds as H2S, SO2, COS, CS2 . . . , in a quantity of up to 15% wt; particularly gases emanating from the Claus process: A first hydrogenation of the sulfur compounds into H2S, the hydrogenation gas being used to regenerate a deactivated bed of oxidation catalyst, both being carried out at 200-500° C. After sulfur removal, the resulting gas undergoes a second hydrogenation step and then a direct oxidation step, said step being operated under the dew point of sulfur to trap the formed sulfur in the catalyst. In the further cycle, the gas streams are switched so as to regenerate the catalyst in run which is deactivated.

Abstract: In a column provided with internals for liquid/gas contacting, the sour water feedstock is stripped using steam, then cooled by a cold liquid and washed using cold water injection. This method allows to separate an ammonia-poor (5-5000 ppm) H2S gaseous effluent and an H2S-lean (100-1000 ppm for example) purified water. The method is yet improved by adding a second column that receives the purified water from the first column and separates the hydrogen sulfide and the ammonia according to the method operated in the first column. The purified water from the second column is preferably partially injected into the first and/or the second column as wash water. A facility for implementing the method according to the invention.

Abstract: A process for removing sulfur from a gas containing sulfur compounds as H2S, SO2, COS, CS2 . . . , in a quantity of up to 15% wt; particularly gases emanating from the Claus process: A first hydrogenation of the sulfur compounds into H2S, the hydrogenation gas being used to regenerate a deactivated bed of oxidation catalyst, both being carried out at 200-500° C. After sulfur removal, the resulting gas undergoes a second hydrogenation step and then a direct oxidation step, said step being operated under the dew point of sulfur to trap the formed sulfur in the catalyst. In the further cycle, the gas streams are switched so as to regenerate the catalyst in run which is deactivated.

Abstract: The invention concerns a flexible process for purifying a solvent which inhibits the formation of hydrates during gas processing, in particular monoethylene glycol (MEG), said solvent having a boiling point which is higher than that of water and, at least at one point in time, being mixed with water and salts, the process operating in a different manner with the same facility as a function of the quantity of salts in the MEG to be treated. The process operates in accordance with a phase known as reclaiming (separation of salts under vacuum followed by vacuum distillation) when the salts content exceeds the precipitation threshold and if not, the process operates in a regeneration phase (absence of separation of salts and no operation under vacuum). Advantageously, the change is made under the control of means for testing the salts.

Abstract: Method of regenerating a glycol solution containing water, hydrocarbons and salts. The glycol solution is expanded in drum (2), then distilled in column (7). The concentrated glycol collected at the level of reboiler (8) is placed under vacuum to vaporize the water and to precipitate the salts. The salts are separated from the glycol in separation device (13). The concentrated glycol freed of the salts is stored in capacity (16).

Abstract: In a process using a hydrophilic liquid desiccant, for dehydrating a gas containing water with regeneration of the steps of: (a) absorbing water by contact between the moist gas and regenerated liquid desiccant from step c), producing a dry gaseous effluent and a stream of liquid desiccant charged with water and absorbed gases; (b) regenerating the liquid desiccant charged with water in a regeneration zone constituting a reboiling zone and a distillation zone, the charged liquid desiccant being sent to said distillation zone, from which a vapor containing water leaves overhead and from which liquid desiccant still containing water leaves from the bottom in the reboiling zone; (c) passing the liquid desiccant from the reboiling zone of step b) and still containing water to an absorption zone, in which the water in the desiccant is vaporized and the water vapor is absorbed by a fraction of regenerated or non regenerated desiccant, passing the resultant desiccant which has absorbed water vapor to the reboiling z