Abstract: A system is arranged to remove carbon dioxide (CO2) from a gas stream by bringing the gas stream into contact with a circulating ammoniated solution stream such that CO2 is removed from the gas stream by the ammoniated solution stream. A method of removing non-volatile compounds from the circulating ammoniated solution stream includes: introducing a portion of the circulating ammoniated solution stream into a gas-liquid separating device; and separating the introduced ammoniated solution into an ammonia rich gas phase and a liquid phase comprising the non-volatile compounds; and reintroducing the ammonia rich gas phase into the circulating ammoniated solution stream.

Abstract: A system and method for operating a stripper tower is disclosed. The temperature TM of an aqueous solution is measured at a first elevation in the stripper tower. Temperature TC, which corresponds to the temperature of saturated steam at the operating pressure of the stripper tower, is calculated. A temperature TOVER, the difference between a temperature of an aqueous solution in the stripper tower subject to over stripping conditions and a temperature of an aqueous solution in the stripper tower subject to normal stripping conditions. The method further includes the step of adjusting a flow rate of saturated steam into the stripper tower so that TM is substantially equivalent to the difference between TC and TOVER.

Abstract: A process of CO2 removal from a flue gas, comprising: (a) contacting a flue gas with a CO2 lean ammonia-comprising medium to produce a CO2 rich ammonia-comprising medium; (b) heating the CO2 rich ammonia-comprising medium to produce a regenerated CO2 lean ammonia-comprising medium; and (c) supplying the regenerated CO2 lean ammonia-comprising medium to said absorber; (d) identifying a desired mole ratio of ammonia to CO2 of the CO2 lean ammonia-comprising medium; (e) predicting a desired temperature of regenerated CO2 lean ammonia-comprising medium present in a sump of a regeneration vessel or predicting a desired operating pressure of a regeneration vessel; (f) controlling the temperature of regenerated CO2 lean ammonia-comprising medium present in the sump of the regeneration vessel or the operating pressure of the regeneration vessel. A system for removal of CO2 from a flue gas, comprising: i.a. a control unit.

Abstract: A method for removal of CO2 from a flue gas stream, comprising the steps of: a) contacting a flue gas stream comprising CO2 with a first absorption liquid comprising NH3 such that the flue gas stream is depleted in CO2; b) contacting the flue gas stream depleted in CO2 of step a) with a second absorption liquid such that NH3 from the flue gas stream is absorbed in said second absorption liquid to form a flue gas stream depleted in CO2 and NH3; c) separating NH3 from the second absorption liquid such that a gas stream comprising NH3 is obtained; d) contacting said gas stream comprising NH3 separated in step c) with a third absorption liquid such that NH3 is absorbed in said third absorption liquid. A system for removal of CO2 from a flue gas stream, the system comprising: a CO2 absorption stage; an NH3 absorption stage; and a reabsorption stage.

Abstract: The present invention relates to a gas cleaning system for cleaning a gas stream containing carbon dioxide and sulfur dioxide, said gas cleaning system comprising: a pre-conditioning section (3); a CO2 removal stage (5); and a post-conditioning section (4); said pre-conditioning section comprising at least two gas-liquid contacting devices (19,20) arranged upstream of the CO2 removal stage (5) with respect to the flow direction of the gas; and said post-conditioning section comprising at least two gas-liquid contacting devices (30,31) arranged downstream of the CO2 removal stage with respect to the flow direction of the gas.

Abstract: Systems and process for volatile degradation removal from amine plant wash water are provided. The systems and processes include a separation device disposed within a water circulation loop and configured to continuously remove at least a portion of the volatile degradation products from the wash solutions. The separation device can be configured for stripping, distillation, and/or extraction of the volatile degradation products from at least a fraction of the spent wash water. Optionally, a chemical agent can be reacted with the volatile degradation products to form heat stable salts for subsequent removal.

Abstract: A system is arranged to remove carbon dioxide (CO2) from a gas stream by bringing the gas stream into contact with a circulating ammoniated solution stream such that CO2 is removed from the gas stream by the ammoniated solution stream. A method of removing non-volatile compounds from the circulating ammoniated solution stream includes: introducing a portion of the circulating ammoniated solution stream into a gas-liquid separating device; and separating the introduced ammoniated solution into an ammonia rich gas phase and a liquid phase comprising the non-volatile compounds; and reintroducing the ammonia rich gas phase into the circulating ammoniated solution stream.

Abstract: In a process for obtaining CO2, desulfurized natural gas or gas which accompanies mineral oil is reformed autothermally with addition of oxygenous gas at a temperature of from 900 to 1200° C. and a pressure of from 40 to 100 bar (a) by partial catalytic oxidation to give a crude synthesis gas, and then converted catalytically to H2 and CO2 at a temperature of from 75 to 110 DEG C. and a pressure of from 50 to 75 bar (a) of CO, CO2 is scrubbed out of the synthesis gas obtained with methanol at a pressure of from 15 to 100 bar (a) and a temperature of from +10 to ?80° C., and the absorbed CO2 is recovered by decompression. A further possible use of the process consists in converting the recovered CO2 to the supercritical state.

Abstract: A process for removal of CO2 from a gas stream, comprising the steps of: (a) contacting in a CO2 absorption stage a gas stream comprising CO2 with a first absorption liquid comprising ammonia; (b) passing used absorption liquid resulting from step (a) to regeneration; (c) regenerating the first absorption liquid by releasing CO2 from used absorption liquid and returning the first absorption liquid to step (a); (d) supplying CO2 released from step (c) to a second absorption liquid; (e) contacting in a contaminant absorption stage the gas stream leaving step (a) with the second absorption liquid; and (f) withdrawing a portion of used absorption liquid resulting from step (e) and passing said liquid portion to regeneration in step (c), before recycling used absorption liquid resulting from step (e) as second absorption liquid to step (d).

Abstract: From the CO2-containing stream of process gas obtained in a process for the treatment of a CO2-containing stream of process gas, which is obtained in the production of pure synthesis gas from raw gas in the partial oxidation of heavy oils, petroleum coke or wastes, or in the gasification of coal, or when processing natural gas or accompanying natural gas, CO2 is removed physisorptively or chemisorptively, and the solvent loaded with CO2 is expanded to a lower pressure for the desorption of CO2. In order to generate CO2 as pure as possible, the contaminated CO2 is condensed to at least 60 bar[a] or below its critical temperature to at least 70 bar[a], and the impurities contained in the liquid CO2 are removed by stripping with gaseous CO2 guided in counterflow.

Abstract: A method for removal of CO2 from a flue gas stream, comprising the steps of: a) contacting a flue gas stream comprising CO2 with a first absorption liquid comprising NH3 such that the flue gas stream is depleted in CO2; b) contacting the flue gas stream depleted in CO2 of step a) with a second absorption liquid such that NH3 from the flue gas stream is absorbed in said second absorption liquid to form a flue gas stream depleted in CO2 and NH3; c) separating NH3 from the second absorption liquid such that a gas stream comprising NH3 is obtained; d) contacting said gas stream comprising NH3 separated in step c) with a third absorption liquid such that NH3 is absorbed in said third absorption liquid. A system for removal of CO2 from a flue gas stream, the system comprising: a CO2 absorption stage; an NH3 absorption stage; and a reabsorption stage.

Abstract: In a process for obtaining CO2, desulfurized natural gas or gas which accompanies mineral oil is reformed autothermally with addition of oxygenous gas at a temperature of from 900 to 1200° C. and a pressure of from 40 to 100 bar (a) by partial catalytic oxidation to give a crude synthesis gas, and then converted catalytically to H2 and CO2 at a temperature of from 75 to 110 DEG C. and a pressure of from 50 to 75 bar (a) of CO, CO2 is scrubbed out of the synthesis gas obtained with methanol at a pressure of from 15 to 100 bar (a) and a temperature of from +10 to ?80° C., and the absorbed CO2 is recovered by decompression. A further possible use of the process consists in converting the recovered CO2 to the supercritical state.

Abstract: The present invention relates to a methods and systems for the removal of contaminants from a gas stream, comprising the steps of: a)introducing CO2 into a wash water stream to obtain a CO2 enriched wash water; and b) contacting said CO2 enriched wash water with the gas stream containing contaminants to be removed to allow absorption of the contaminants into the CO2 enriched wash water. The present invention further relates to the use of CO2 enriched wash water for removal of alkaline contaminants from a gas stream in a gas purification system.

Abstract: A hydrocarbon gas containing H2S, mercaptans and CO2 is fed to an absorption plant operated at a pressure of 20 to 80 bar and supplied with a selective solvent, a solvent stream loaded with H2S and a roughly desulfurized gas stream are withdrawn, the H2S loaded solvent stream is charged to a regeneration plant and the roughly desulfurized gas stream is charged to an absorption and regeneration plant operated at a pressure of 20 to 80 bar, a large first gas stream of H2S and CO2 and an unloaded solvent stream are withdrawn from the absorption regeneration plant, and the large first gas steam of H2S and CO2 is supplied to a Claus plant, and a valuable hydrocarbon gas stream is withdrawn from the absorption and regeneration plant.

Abstract: This invention relates to a process of cleaning gas, in particular hydrocarbonaceous gas such as e.g. natural gas, which is contaminated with sulfur in the form of H2S and mercaptans as well as CO2.

Abstract: A process for producing propylene from methanol, wherein methanol vapor is reacted on a first catalyst to obtain a first vapor mixture containing dimethyl ether (DME), which is reacted on a form-selective zeolite catalyst disposed as bed in at least two series-connected shaft reactors to produce a product mixture containing propylene.

Abstract: This invention relates to a process of producing C2- to C4-olefins from steam and a feed mixture containing C4- to C8-olefins, wherein the feed mixture containing steam is introduced into a reactor with an inlet temperature of 300 to 700° C., said reactor comprising a bed of granular, form-selective zeolite catalyst, and wherein a product mixture containing steam and C2- to C4-olefins is withdrawn from the bed and is passed through at least one cooling means.

Abstract: The feed hydrocarbon together with steam is passed as vapor through a thermal steam cracking in which it is heated to temperatures in the range from 700 to 1000° C., where a cracking mixture is produced which contains C2- to C6-olefins and C4- to C6-diolefins. From the cracking mixture a first fraction, which contains C2- and C3-olefins, and a second fraction, which contains olefins and diolefins of the range C4 to C6, are separated. The diolefins are at least partly removed from the second fraction, and an intermediate product is produced which consists of C4- to C6-olefins for at least 30 wt-%. A feed mixture containing C4- to C6-olefins and steam is introduced into a reactor with an inlet temperature of 300 to 700° C., which reactor contains a bed of granular, form-selective catalyst, where a product mixture containing C2- to C4-olefins is withdrawn from the bed and C2- and C3-olefins are separated from the product mixture.

Abstract: Methanol vapor is reacted on a first catalyst to obtain a first vapor mixture containing dimethyl ether (DME), and from the first vapor mixture a product mixture containing propylene is produced on a form-selective zeolite catalyst. The form-selective zeolite catalyst is disposed as bed in at least two series-connected shaft reactors. A first partial stream of the DME-containing first vapor mixture is introduced into the first shaft reactor together with steam, from the first shaft reactor a first intermediate product mixture is withdrawn and charged into the second shaft reactor, a second partial stream of the DME-containing first vapor mixture also being supplied to the second shaft reactor. From the last one of the series-connected shaft reactors a product mixture is withdrawn and a fraction rich in propylene is separated, where there are obtained residual substances which are in part gaseous. At least part of the residual substances is recirculated to at least one of the shaft reactors.