Systems and processes for upgrading natural gas liquids (NGL). A natural gas, preferably a shale gas, comprising methane and one or more natural gas liquids can be converted to one or more liquid hydrocarbons. Methane can be separated from the one or more liquid hydrocarbons using a liquid absorbent to provide a first separated stream comprising the methane from the converted stream and a second separated stream comprising the one or more liquid hydrocarbons from the converted stream. At least a portion of the one or more liquid hydrocarbons can be recycled as the liquid absorbent.

Provided are an apparatus and a method for separation and recovery of propane and heavier hydrocarbons from LNG. The apparatus has, from the upstream side toward the downstream side of LNG supply, first column (3) equipped with first column overhead condenser (2), first column bottom reboiler (4) and side reboiler (5), and second column (14) equipped with second column overhead condenser (11) and second column bottom reboiler (15). The first column (3) separates methane and a part of ethane as an overhead vapor and separates remaining ethane and C3 or higher hydrocarbons as a bottom liquid. The second column (14) separates ethane as an overhead vapor and separates C3 or higher hydrocarbons as a bottom liquid.

Provided are an apparatus and a method for separation and recovery of propane and heavier hydrocarbons from LNG. The apparatus has, from the upstream side toward the downstream side of LNG supply, first column (3) equipped with first column overhead condenser (2), first column bottom reboiler (4) and side reboiler (5), and second column (14) equipped with second column overhead condenser (11) and second column bottom reboiler (15). The first column (3) separates methane and a part of ethane as an overhead vapor and separates remaining ethane and C3 or higher hydrocarbons as a bottom liquid. The second column (14) separates ethane as an overhead vapor and separates C3 or higher hydrocarbons as a bottom liquid.

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. It is provided that, at a first pressure level, the separation feedstock is partially condensed in a single step by cooling from a first temperature level to a second temperature level, thereby obtaining precisely one first liquid fraction and precisely one first gaseous fraction; at least one part of the first gaseous fraction is partially condensed in a single step through further cooling from the second temperature level to a third temperature level, thereby obtaining precisely one second liquid fraction and precisely one second gaseous fraction; at least one part of the second gaseous fraction at the second pressure level is subjected to a contraflow absorption in the contraflow to an absorption liquid containing predominantly methane, thereby obtaining precisely one third liquid fraction and precisely one third gaseous fraction; the first, the second and the third liquid fraction are at least partially combined and, at least partially, at a second pressure level above the first pressure level, subjected to a low-temperature rectification, thereby obtaining a sump liquid and an overhead gas; at least one part of the overhead gas at the second pressure level is partially condensed in a single step through further cooling from the second temperature level to the third temperature level, thereby obtaining a fourth liquid fraction and a fourth gaseous fraction; and the absorption liquid containing predominantly methane is formed through further cooling of at least a part of the fourth gaseous fraction to a fourth temperature level. A corresponding plant also forms the subject matter of the invention.

A process (10) for the recovery of hydrocarbons from a Fischer-Tropsch tail gas includes providing a hydrocarbon rich Fischer-Tropsch tail gas (30) which includes hydrocarbons and carbon dioxide, compressing (14) the hydrocarbon rich Fischer-Tropsch tail gas (30) to provide a compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54), and contacting the compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54) with a lean oil (64, 54) to recover the hydrocarbons from the compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54) and to produce a hydrocarbon rich oil (66). Carbon dioxide is stripped (20) from the hydrocarbon rich oil (66) at a pressure which is below the pressure at which the hydrocarbon rich Fischer-Tropsch tail gas (36, 54) is contacted with the lean oil (64, 54), to provide a stripped hydrocarbon oil product (86).

A process (10) for the recovery of hydrocarbons from a Fischer-Tropsch tail gas includes providing a hydrocarbon rich Fischer-Tropsch tail gas (30) which includes hydrocarbons and carbon dioxide, compressing (14) the hydrocarbon rich Fischer-Tropsch tail gas (30) to provide a compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54), and contacting the compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54) with a lean oil (64, 54) to recover the hydrocarbons from the compressed hydrocarbon rich Fischer-Tropsch tail gas (36, 54) and to produce a hydrocarbon rich oil (66). Carbon dioxide is stripped (20) from the hydrocarbon rich oil (66) at a pressure which is below the pressure at which the hydrocarbon rich Fischer-Tropsch tail gas (36, 54) is contacted with the lean oil (64, 54), to provide a stripped hydrocarbon oil product (86).

Described herein are methods and systems for performing liquid-liquid extraction in bulk tankage. According to certain embodiments, the liquid-liquid extraction can occur in a bulk tank via a circulation loop, in which a solvent mixture is injected with the hydrocarbon ahead of mix valves on the circulation loop. According to other embodiments, a misting system is installed in the vapor or head space of bulk tankage. The misting system distributes small micro-drops of a solvent mixture so as to cause a uniform lay down over the entire top surface area of hydrocarbon. The solvent mixture migrates from the top surface of the hydrocarbon to the bottom of the bulk tank, reacting during migration to cause liquid-liquid extraction.

Described herein are methods and systems for performing liquid-liquid extraction in bulk tankage. According to certain embodiments, the liquid-liquid extraction can occur in a bulk tank via a circulation loop, in which a solvent mixture is injected with the hydrocarbon ahead of mix valves on the circulation loop. According to other embodiments, a misting system is installed in the vapor or head space of bulk tankage. The misting system distributes small micro-drops of a solvent mixture so as to cause a uniform lay down over the entire top surface area of hydrocarbon. The solvent mixture migrates from the top surface of the hydrocarbon to the bottom of the bulk tank, reacting during migration to cause liquid-liquid extraction.

A natural gas liquids (NGL) plant, the NGL plant comprising an absorber configured to provide an absorber overhead and an absorber bottoms, a stripper configured to produce a stripper overhead and a stripper bottoms, wherein the stripper is positioned downstream from the absorber and fluidly connected therewith such that the absorber bottoms can be introduced into the stripper, and a multi-pass heat exchanger configured to provide at least one reflux stream to the absorber, wherein the absorber and stripper are configured, in an ethane rejection arrangement, to provide the stripper overhead to a top of the absorber, and wherein the absorber and stripper are configured, in an ethane recovery arrangement, to provide the stripper overhead to a bottom of the absorber.

A natural gas liquids (NGL) plant, the NGL plant comprising an absorber configured to provide an absorber overhead and an absorber bottoms, a stripper configured to produce a stripper overhead and a stripper bottoms, wherein the stripper is positioned downstream from the absorber and fluidly connected therewith such that the absorber bottoms can be introduced into the stripper, and a multi-pass heat exchanger configured to provide at least one reflux stream to the absorber, wherein the absorber and stripper are configured, in an ethane rejection arrangement, to provide the stripper overhead to a top of the absorber, and wherein the absorber and stripper are configured, in an ethane recovery arrangement, to provide the stripper overhead to a bottom of the absorber.