Abstract: The invention relates to a method (100) for the recovery of a separation product which contains predominantly hydrocarbons with two carbon atoms, with the use of a separation feedstock which contains predominantly methane, hydrogen and hydrocarbons with two carbon atoms, wherein the methane content of the separation feedstock is up to 20%, and the separation feedstock is provided in a gaseous state.

Abstract: Proposed is a process for producing ethylene wherein using a dehydrogenation of ethane a process gas containing at least ethane, ethylene and compounds having a lower boiling point than ethane and ethylene is formed, wherein using at least a part of the process gas a separation input is formed and subjected to a low-temperature separation (6) in which the separation input is cooled and in which one or more condensates are separated from the separation input, wherein the condensate(s) are at least partly subjected to a low-temperature rectification to obtain a gaseous first fraction and a liquid second fraction, wherein the gaseous first fraction contains at least the ethane and the ethylene in a lower proportion than in the separation input and the compounds having a lower boiling point than ethane and ethylene in a higher proportion than in the separation input.

Abstract: The invention relates to a method (100) for the recovery of a separation product which contains predominantly hydrocarbons with two carbon atoms, with the use of a separation feedstock which contains predominantly methane, hydrogen and hydrocarbons with two carbon atoms, wherein the methane content of the separation feedstock is up to 20%, and the separation feedstock is provided in a gaseous state.

Abstract: The present invention relates to a process (100) for separatory processing of a starting mixture containing predominantly hydrogen, methane and hydrocarbons having two or two or more carbon atoms, wherein at least a portion of the starting mixture is cooled to form one or more condensates using one or more heat exchangers (101, 103, 105, 107) and at least a portion of the condensate(s) is subjected to a rectification to form a gaseous methane-rich fraction. It is provided that the gaseous methane-rich fraction is used to form a first fluid stream which is at least partly compressed, in an unchanged composition with respect to the gaseous methane-rich fraction, to a liquefaction pressure level of 35 to 45 bar, and at least partly liquefied by cooling, and in that the first fluid stream, or a second fluid stream formed using the first fluid stream, is expanded to a delivery pressure and heated in the or at least one of the heat exchanger(s) (101, 103, 105, 107).

Abstract: Proposed is a process for producing ethylene wherein using a dehydrogenation of ethane a process gas containing at least ethane, ethylene and compounds having a lower boiling point than ethane and ethylene is formed, wherein using at least a part of the process gas a separation input is formed and subjected to a low-temperature separation (6) in which the separation input is cooled and in which one or more condensates are separated from the separation input, wherein the condensate(s) are at least partly subjected to a low-temperature rectification to obtain a gaseous first fraction and a liquid second fraction, wherein the gaseous first fraction contains at least the ethane and the ethylene in a lower proportion than in the separation input and the compounds having a lower boiling point than ethane and ethylene in a higher proportion than in the separation input.

Abstract: To obtain hydrogen from a gaseous C2minus feed, it is cooled from a first to a second temperature level at a first pressure level forming one or more condensates. A gaseous remainder is cooled to a third temperature level and subjected to a counterflow absorption at the first pressure level, obtaining a top gas rich in hydrogen and methane and a sump liquid. The former is heated and subjected to pressure swing adsorption at the first pressure level, forming a product stream rich in hydrogen and depleted in or free from methane. The condensate(s) and/or the sump liquid is/are expanded to and fed into a low pressure demethanizer at the second pressure level. The counterflow absorption is carried out using fluid taken from the demethanizer at the second pressure level, compressed in gaseous form to the first pressure level and cooled to the third temperature level.

Abstract: A method (100, 200) is proposed for obtaining hydrogen from a gaseous feed mixture rich in hydrogen, methane and hydrocarbons having two carbon atoms, wherein fluid of the feed mixture is cooled from a first temperature level to a second temperature level at a first pressure level such that one or more condensates are precipitated out of the fluid of the feed mixture, leaving a residual gas, fluid of the residual gas is further cooled to a third temperature level and subjected to a counterflow absorption at the first pressure level, thereby obtaining a top gas rich in hydrogen and methane and a sump liquid, fluid of the top gas is heated and subjected to pressure swing adsorption (9) at the first pressure level, to form a product stream which is rich in hydrogen and depleted in or free from methane, and fluid of the condensate or condensates and/or of the sump liquid is expanded from the first pressure level to a second pressure level and is fed into a low pressure demethanizer at the second pressure level.

Abstract: In a process for producing olefins, a hydrocarbon-containing feed is fed into a cracking furnace where relatively long-chain hydrocarbons of the hydrocarbon-containing feed are cracked at least partly to form shorter-chain olefins, encompassing ethylene and propylene. Cracking gas (1) formed during cracking is conveyed in succession through an upper section (11) and a lower section (12) of a scrubbing column (10) in countercurrent to a liquid scrubbing medium (43, 31), is proposed. A fraction (43) rich in petroleum spirit is used in the lower section (11) of the scrubbing column (10) and a water-rich fraction (31) is used in the upper section (11) of the scrubbing column (10) as scrubbing medium (43, 31). A plant configured for carrying out the process is likewise provided by the present invention.

Abstract: The invention describes a method for separating hydrocarbons in an installation for generating hydrocarbons from a hydrocarbon-containing charge by cleavage. The product gas of the cleavage, which contains gaseous hydrocarbons, is compressed, dried, and supplied as charge material into a separation stage (a front end C3/C4 separation). The front end C3/C4 separation comprises a C4 absorber and a depropanizer. A hydrocarbon fraction consisting of hydrocarbons having a maximum of 3 carbon atoms is obtained as a gaseous overhead product of the C4 absorber. A liquid hydrocarbon fraction consisting of hydrocarbons having at least 4 carbon atoms is obtained as a bottom product of the depropanizer. The front end C3/C4 separation comprises an additional process technological C2/C4 separation stage is arranged between the C4 absorber and the depropanizer.

Abstract: A process for producing olefins, in which a hydrocarbon-containing feed is fed into a cracking furnace where relatively long-chain hydrocarbons of the hydrocarbon-containing feed are cracked at least partly to form shorter-chain olefins, encompassing ethylene and propylene. Cracking gas (1) formed during cracking is conveyed in succession through an upper section (11) and a lower section (12) of a scrubbing column (10) in countercurrent to a liquid scrubbing medium (43, 31), is proposed. A fraction (43) rich in petroleum spirit is used in the lower section (11) of the scrubbing column (10) and a water-rich fraction (31) is used in the upper section (11) of the scrubbing column (10) as scrubbing medium (43, 31). A plant configured for carrying out the process is likewise provided by the present invention.

Abstract: To decrease capital costs of crack gas treatment of the olefin plant, a method for separation of olefins reduces the units for catalytic hydrogenation. In the method, olefins having three carbon atoms are separated from olefins having four carbon atoms. Crude gas is precompressed (1), precooled and dried (2), and passed into a C3/C4 separation stage (6) comprising a C4 absorber, operating at full crude gas pressure, and a depropanizer, operated at a pressure of 8 to 12 bar. In the C3/C4 separation stage, the olefins are separated into a fraction having at most three carbon atoms (C3?), and a fraction having at least four carbon atoms (C4+). The fraction having at most three carbon atoms is completely compressed (1) and passed to the catalytic hydrogenation (4); the fraction having at least four carbon atoms is passed out for further processing (7).

Abstract: A method is described for refrigerant supply of a low-temperature separation stage in a plant for producing olefins from hydrocarbon-containing feed (olefin plant). During the separation sequence beginning with a front end deethanizer (3) downstream of raw gas compressor (1), precooler and dryer (2), first separation is performed into an olefin fraction having at most two carbon atoms and an olefin fraction having at least three carbon atoms. The fraction having at least three carbon atoms is conducted to the further separation sequence for longer-chain olefins (4). The fraction having at most two carbon atoms is conducted via a catalytic hydrogenation stage (5) connected in between to the low-temperature separation stage (6) which comprises three condensation stages in the temperature range from ?50° C. to ?100° C.

Abstract: A method is described for refrigerant supply of a low-temperature separation stage in a plant for producing olefins from hydrocarbon-containing feed (olefin plant). During the separation sequence beginning with a front end deethanizer (3) downstream of raw gas compressor (1), precooler and dryer (2), first separation is performed into an olefin fraction having at most two carbon atoms and an olefin fraction having at least three carbon atoms. The fraction having at least three carbon atoms is conducted to the further separation sequence for longer-chain olefins (4). The fraction having at most two carbon atoms is conducted via a catalytic hydrogenation stage (5) connected in between to the low-temperature separation stage (6) which comprises three condensation stages in the temperature range from ?50° C. to ?100° C.