Abstract: The invention relates to a process and device for the cryogenic separation of a methane-containing feed gas predominantly consisting of hydrogen and carbon monoxide, that is partially condensed in this case by cooling, in order to obtain a hydrogen-containing first liquid phase predominantly consisting of carbon monoxide and methane, from which first liquid phase, in an H2 separation column that is heated via a circulation heater, a second liquid phase is generated by separating off hydrogen, from which second liquid phase, in a CO/CH4 separation column, a carbon monoxide-rich gas phase is obtained having a purity that permits release thereof as carbon monoxide product. It is characteristic in this case that a low-methane material stream is withdrawn from the H2 separation column and is then applied to the CO/CH4 separation column as reflux.

Abstract: A process for facile separation of lighter hydrocarbon fractions from the heavier fractions of hydrocarbon oil feedstocks is disclosed, which utilizes novel sparging and reverse distillation techniques. The present invention can be utilized for the facile “topping” of crude oil extracted on-site. Moreover, while heavier hydrocarbon fractions may be shipped to refineries for further processing, this invention will also prove useful for quick separation of light fractions produced by cracking processes off-site.

Abstract: Method for concentrating components through a distillation column are disclosed. A process stream is provided containing hydrocarbons, carbon dioxide, and water. The process stream is passed into the distillation column at a bottom portion of the distillation column. The process stream is fractionally distilled in the distillation column, forming an overhead vapor stream, a middle fluid stream, and a bottoms liquid stream. The middle fluid stream is removed from a middle location of the distillation column. The bottoms liquid stream is removed from the distillation column. The overhead vapor stream is removed from the distillation column. The middle fluid stream consists of a first portion of the carbon dioxide and a first portion of the hydrocarbons. The bottoms liquid stream consists of a second portion of the hydrocarbons as a first phase and substantially all the water as a second phase.

Abstract: A process for removing light components from an ethylene stream may include providing a dried ethylene stream containing ethylene, ethane, CO, CO2, H2, CH4, and C3+ hydrocarbons. The process may include sending the dried ethylene stream to a stripper to produce an overhead stream containing ethylene, CO, H2 and CH4, and a bottom stream containing ethylene, ethane, CO2, and C3+ hydrocarbons. The gaseous phase on top of the stripper may be condensed in a heat exchanger cooled by a refrigerant stream to get a first gaseous phase and a first liquid phase. The first gaseous phase may be condensed in a heat exchanger cooled by liquid ethane or liquid ethylene to get a second gaseous phase containing ethylene CO, H2 and CH4 and a second liquid phase. The first and second liquid phases may be the reflux of the stripper.

Abstract: The present invention relates to a method of liquefying a hydrocarbon stream such as a natural gas stream, the method at least comprising the steps of: supplying a partly condensed hydrocarbon feed stream (10) to a first gas/liquid separator (2); separating the feed stream (10) in the first gas/liquid separator (2) into a gaseous stream (20) and a liquid stream (30); expanding the gaseous stream (20) thereby obtaining an expanded stream (40) and feeding it (40) into a second gas/liquid separator (3); feeding the liquid stream (30) into the second gas/liquid separator (3); removing from the bottom of the second gas/liquid separator a liquid stream (60) and feeding it into a fractionation column (5); removing from the top of the second gas/liquid separator (3) a gaseous stream (50) and passing it to a compressor (6) thereby obtaining a compressed stream (70); cooling the compressed stream (70) thereby obtaining a cooled compressed stream (80); heat exchanging the cooled compressed stream (80) against a stream b

Abstract: The present invention relates to an improved process for recovery of natural gas liquids from a natural gas feed stream. The process runs at a constant pressure with no intentional reduction in pressure. An open loop mixed refrigerant is used to provide process cooling and to provide a reflux stream for the distillation column used to recover the natural gas liquids. The processes may be used to recover C3+ hydrocarbons from natural gas, or to recover C2+ hydrocarbons from natural gas.

Abstract: A separation method using a column with cross-corrugated structured packing for separating a gas mixture is presented.

Abstract: A process for separating a helium-rich fraction from a liquefied natural gas stream, is disclosed. In an embodiment, the process includes expansion of a liquefied natural gas stream and separation of the helium-rich fraction. The helium-rich fraction is heated countercurrent to a natural gas stream to be cooled and liquefied. The natural gas stream liquefied in a heat exchange countercurrent to the helium-rich fraction to be heated is fed prior to and/or in the separation of the helium-rich fraction. The total enthalpy of the mixture of the two aforementioned natural gas streams brought to the separation of the helium-rich fraction is variable.

Abstract: A process for the recovery and purification of ethylene and optionally propylene from a stream containing lighter and heavier components that employs an ethylene distributor column and a partially thermally coupled distributed distillation system.

Abstract: An improved apparatus and method for providing reflux to a refluxed heavies removal column of a LNG facility. The apparatus comprises stacked vertical core-in-kettle heat exchangers and an economizer disposed between the heat exchangers. The reflux stream originates from the methane-rich refrigerant of the methane refrigeration cycle. The liquid reflux stream generated by cooling the methane-rich stream in the vertical heat exchangers via indirect heat exchange with an upstream refrigerant.

Abstract: A process and apparatus for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbons from a liquefied natural gas (LNG) stream is disclosed. The LNG feed stream is directed in heat exchanger relation with a warmer distillation stream rising from the fractionation stages of a distillation column, whereby the LNG feed stream is partially heated and the distillation stream is partially condensed. The partially condensed distillation stream is separated to provide volatile residue gas and a reflux stream, whereupon the reflux stream is supplied to the column at a top column feed position. A portion of the partially heated LNG feed stream is supplied to the column at an upper mid-column feed point, and the remaining portion is heated further to partially or totally vaporize it and thereafter supplied to the column at a lower mid-column feed position.

Abstract: Process and apparatus for separation of LNG allow both maximum enriching of the methane product in methane at any initial LNG composition, and to production the methane product in fully liquid state for the customer.

Abstract: Dephlegmator system without headers, collectors, or distributors at the bottom end of feed circuits in plate and fin exchangers operating in condensing or rectifying service. Each dephlegmator is installed within a pressure vessel, thereby eliminating the need for headers, collectors, or distributors at the bottom end of the feed circuits. In an alternative embodiment of the invention, upper and lower segments of the pressure vessel are isolated by a mid-vessel seal between the vessel and dephlegmator walls, and headers or collectors are not required at the upper and lower ends of the feed circuits.

Abstract: A cryogenic process for the separation of one light gas component from a heavier gas component in a gas feed stream, by injecting a liquid hydrocarbon additive stream into the top or upper portion of a dephlegmator-heat exchanger, to increase the rectification temperature, or to maintain the temperature and reduce the additive flow rate relative to the respective values required with a conventional, single stage condenser.

Abstract: C2 and C3 hydrocarbons, particularly ethylene and propylene, are recovered from refinery or petrochemical plant gas mixtures by cooling and fractionating a feed gas mixture containing these hydrocarbons and lighter components. Refrigeration for the process is provided by a closed-loop gas expander refrigeration process cycle which preferably uses nitrogen as the recirculating refrigerant. Cooling and fractionation may be effected in a dephlegmator.

Abstract: A dephlegmator includes a feed gas passage and a refrigerant passage. A feed gas introduced into the feed gas passage from the bottom is heat-exchanged with a refrigerant passing through the refrigerant passage. Components having low boiling points are withdrawn as rectified gases from the top, and components having high boiling points are discharged as condensates from the bottom. The refrigerant passage is divided into a first section on the top side and a second section on the bottom side by a bridgewall. In the first section, a liquid or gas-liquid two-phase refrigerant is introduced from the bottom of the refrigerant passage so as to flow parallel to the feed gas. In the second section, a gas fraction of the refrigerant discharged from the first section flows.

Abstract: An improved condensating-fractionating tower system used in the separation of gaseous mixture, comprising a dephlegmator, a column section and a tower bottom, the said dephlegmator being provided in the upper portion of the tower, is characterized in that the dephlegmator is a plate-fin dephlegmator.

Abstract: A high purity methane product is recovered from a feed gas mixture containing methane and one or more hydrocarbons heavier than methane by cooling, condensing, and rectifying the feed in a dephlegmator. The high purity methane product, containing at least 98 mole % methane, can be liquefied and stored for use as a fuel for internal combustion engines. A hydrocarbon product containing components heavier than methane is also recovered.Methane recovery and C.sub.2.sup.+ hydrocarbon product purity can be improved by the use of a combined stripping heat exchanger and feed gas cooler. External refrigeration is utilized and can be supplemented in part by autorefrigeration provided by vaporizing dephlegmator liquid.

Abstract: A single or double dephlegmator is used to transfer heat between condensing nitrogen and rich liquid in a single column nitrogen generator.

Abstract: Nitrogen is removed from a pressurized feed gas mixture containing nitrogen and methane by cooling, partial condensation, and rectification in one or more dephlegmators. Autorefrigeration is provided by pressure letdown of selected process streams and external refrigeration is not required.

Abstract: A process and system for providing cooling service (refrigerant) for a gas separation process wherein the refrigerant is obtained from the system process fluid and after serving as refrigerant is returned to the process side for separation into product.

Abstract: Olefins are recovered from thermally cracked gas or fluid catalytic cracking off gas by cooling the gas to condense a portion of the hydrocarbons, removing hydrogen from the noncondensed gas, and condensing the remaining hydrocarbons in a cold condensing zone using a dephlegmator which operates above about -166.degree. F. This mode of operation minimizes the amount of methane in the condensate which is further processed in demethanizer column(s) and permits the condensation of ethylene at warmer temperatures than possible using a partial condenser in the cold condensing zone. The use of a dephlegmator at temperatures above about -166.degree. F. minimizes or eliminates the formation and accumulation of unstable nitrogen compounds in the ethylene recovery system. Hydrogen is removed from the noncondensed gas in a process selected from polymeric membrane permeation, adsorptive membrane permeation, or pressure swing adsorption.

Abstract: In this process, which incorporates an integral cascade, the coolant mixture issuing from the penultimate stage (1B) of the compressor cycle (1) is delivered to a distillation apparatus (5) the head vapor of which is cooled (in 24) to a temperature significantly lower than the ambient temperature, then separated into two phases (in 6C); the vapor stage is supplied to the last stage (1C) of the compressor, and the liquid phase constitutes a coolant fluid for the hot part (8) of the heat exchange line (7).