Abstract: An oil conditioning unit includes a pump for receiving unstabilized crude oil at a first pressure and pumping the unstabilized crude oil at a second pressure higher than the first pressure, a first pre-heater downstream of the pump for heating the unstabilized crude oil to a first temperature, and a degassing vessel downstream of the first pre-heater. The degassing vessel is configured to separate light hydrocarbon gases from the unstabilized crude oil at the first temperature to produce stabilized crude oil having a Reid Vapor Pressure less than or equal to 13.7 psia. In some examples, the degassing vessel is configured to produce stabilized crude oil having a Reid Vapor Pressure well below 13.7 psia.

Abstract: A method for stabilizing crude oil includes pumping unstabilized crude oil with a pump from a first pressure to a second pressure higher than the first pressure, heating the unstabilized crude oil from the pump with a pre-heater at a first temperature, and separating light hydrocarbon gases from the unstabilized crude oil in a degassing vessel at the first temperature to produce stabilized crude oil and separated light hydrocarbon gases. The stabilized crude oil has a Reid Vapor Pressure less than or equal to 13.7 psia.

Abstract: An oil conditioning unit includes a pump for receiving unstabilized crude oil at a first pressure and pumping the unstabilized crude oil at a second pressure higher than the first pressure, a first pre-heater downstream of the pump for heating the unstabilized crude oil to a first temperature, and a degassing vessel downstream of the first pre-heater. The degassing vessel is configured to separate light hydrocarbon gases from the unstabilized crude oil at the first temperature to produce stabilized crude oil having a Reid Vapor Pressure less than or equal to 13.7 psia. In some examples, the degassing vessel is configured to produce stabilized crude oil having a Reid Vapor Pressure well below 13.7 psia.

Abstract: The recycle gas stream containing hydrogen that is part of the feedstream to a hydroprocessing reactor is mixed with the low purity make-up hydrogen and the sour flash gases upstream of the recycle gas compressor and compressed by the recycle gas compressor. The compressed gases pass through a methane and higher (C1+) absorber to produce a sweet hydrogen recycle gas stream that is delivered to the hydroprocessing reactor at 96-98 mol % hydrogen. The process can be used to advantage in existing process facilities to increase the hydrogen partial pressure in the feedstream to the hydroprocessor where the existing recycle gas compressor is not designed for compressing the high purity hydrogen.

Abstract: A retro fitted unit to an existing simple refrigerated natural gas plant that substantially increases the amounts of propane, butanes and natural gasoline, or ethane, propane, butanes and natural gasoline recovered from the natural gas in the existing gas treatment plant, wherein in one embodiment the existing natural gas treatment plant includes a refrigerated feed cooler, a separator and a stabilizer and the retrofitted unit comprises an NGL absorber, a refrigerated lean solvent cooler and a lean solvent regenerator; and wherein in a second embodiment the existing simple refrigerated gas treatment plant additionally includes an NGL fractionation train that separates the recovered NGL into saleable fractions and wherein the NGL fractionation train includes a debutanizer that produces all or part of the lean solvent utilized in the retrofitted unit which comprises an NGL absorber and a refrigerated solvent cooler; and wherein the natural gas treatment process utilizes a solvent that is pre-saturated with ligh

Abstract: A process for rejecting reactor byproduct from the polymerization reactor in an olefins polymerization process wherein reactor waste gas stream(s) comprising unreacted monomers, reactor byproduct and light components are treated in an absorption process to additionally recover the monomers. The absorption process comprises contacting the reactor waste gas stream(s) with an absorption solvent in an absorption zone to produce a gas stream comprising the light components, and a liquid stream comprising the absorption solvent, absorbed reactor byproduct and absorbed monomers. The liquid stream is fractionated in a distillation column to produce a distillation column bottoms stream that is the absorption solvent which is conveyed to the absorption zone, and an overhead stream comprising the monomers and reactor byproduct which is further fractionated in a splitter column to reject the reactor byproduct as a bottoms stream. The recovered monomers from the splitter overhead can be conveyed to the reactor.

Abstract: An absorption process for separating a feed gas stream having components with a spectrum of volatilities including volatile (light) components, intermediate volatility components, and least volatile (heavy) components. The disclosed process includes the steps of: (1) contacting the feed gas stream with an internally generated liquid lean solvent stream in an absorber to produce a light product gas stream that is composed of predominantly light components and a rich solvent stream containing most of the intermediate and heavy components; (2) flashing the rich solvent stream at reduced pressure in a flash zone to produce an intermediate product gas stream composed predominantly of intermediate components and a lean solvent stream; (3) conveying the lean solvent stream from the flashing zone to the absorber, wherein the lean solvent is composed predominantly of heavy components supplied from the feed; the process does not use an external lean solvent.

Abstract: An absorption process for recovering hydrogen, ethylene, methane and heavy hydrocarbons from refinery and petrochemical off-gas streams wherein the absorption solvent is comprised of heavy hydrocarbons derived from the off-gas feed stream; no external solvent is used. The process comprises the steps of absorbing ethylene out of the feed off-gas in an absorber stripper using the absorption solvent, and fractionating the rich absorption solvent in a distillation column to produce an ethylene product stream as the overhead stream and the heavy hydrocarbon absorption solvent as the bottoms stream.

Abstract: A process for gas phase polymerization of olefins wherein reactor vent gas stream(s) comprising unreacted monomers and light components are treated in an absorption process to recover the monomers. The absorption process comprises contacting the reactor vent gas stream(s) with an absorption solvent in an absorption zone to produce a gas stream comprising the light components, and a liquid stream comprising the absorption solvent and absorbed monomers. The liquid stream is fractionated in a distillation column to produce a distillation column bottoms stream that is the absorption solvent which is conveyed to the absorption zone, and an overhead stream comprising the monomers which can be conveyed to the reactor. In a preferred embodiment, the absorption solvent consists essentially of components derived from the reactor vent gas stream(s) so that no external solvent is required.

Abstract: An absorption process for separating a feed gas stream having components with a spectrum of volatilities including volatile (light) components, intermediate volatility components, and least volatile (heavy) components. The disclosed process includes the steps of: (1) contacting the feed gas stream with a liquid lean solvent stream in an absorber to produce a light product gas stream that is composed of predominantly light components and a rich solvent stream containing most of the intermediate and heavy components; (2) flashing the rich solvent stream at reduced pressure in a flash zone to produce an intermediate product gas stream composed predominantly of intermediate components and a lean solvent stream; (3) conveying the lean solvent stream from the flashing zone to the absorber, wherein the lean solvent is composed predominantly of heavy components taken from the feed; the process does not use an external lean solvent.

Abstract: A continuous process is described for contacting an olefins-containing feed gas stream, which has been freed of CO.sub.2 and sulfur compounds, compressed, cooled, and dried, with a solvent in an intercooled and reboiled demethanizing absorber to produce a rich solvent bottom stream containing ethylene and heavier hydrocarbons and an absorber overhead stream which is fed to a methane absorber which recovers a hydrogen product stream as overhead and produces a rich solvent stream as bottoms. When recovering up to 50% of the incoming hydrogen, this rich solvent stream from the methane absorber is fed to the demethanizing absorber, but when recovering from 20% to 100% of the incoming hydrogen, this rich solvent stream is recycled in part to the demethanizing absorber and in part is fed to a methane stripper which sends its bottoms to the methane absorber and its overhead to an auto refrigerated recovery unit which removes H.sub.2, CH.sub.4, and CO as a fuel gas product and produces an ethylene and heavier stream.

Abstract: A subquality nitrogen-rich natural gas stream containing more than 0.1 mol % helium is countercurrently extracted with a lean physical solvent to produce a rich solvent bottoms stream which is flashed twice to produce a methane-rich gas product and a nitrogen-helium product which is fed to at least one membrane unit. A reject nitrogen stream and a crude helium stream are discharged from this unit. The crude helium stream is either compressed to a pressure within the range of 200 to 3,000 psia for sale or is compressed to no more than 1,000 psia and fed to a PSA unit which produces a reject nitrogen stream and a highly purified (99.99+ mol %) helium stream which is compressed to a pressure within the range of 200 to 3,000 psia for sale.

Abstract: A continuous process is described for contacting an olefins-containing feed gas stream, freed of CO.sub.2 and sulfur compounds, in a front-end heat-pumped depropanizer to remove the C.sub.

Abstract: A process is described for processing an inert-rich natural gas stream with a lean oil physical solvent to obtain a specification-grade inert gas product, and a specification-grade hydrocarbon gas product, preferably in combination with an existing absorber plant. The process is an adaptation of the extractive flashing and extractive stripping versions of the Mehra Process.

Abstract: A continuous process is disclosed for separating components of a hydrocarbon gas stream which are selected from the group consisting of methane, ethane, higher saturated hydrocarbons, and mixtures thereof by countercurrently contacting the hydrocarbon gas stream with a physical solvent selected from the group consisting of:(1) paraffinic solvents having molecular weights ranging from 75 to 140 and UOP characterization factors ranging from 12.0 to 13.5, these factors being independent of the aromatic content of the paraffinic solvents,(2) naphthenic solvents having molecular weights ranging from 75 to 130 and UOP characterization factors ranging from 10.5 to 12.0, these factors being independent of the aromatic content of the naphthenic solvents, and(3) benzene and toluene,to produce an overhead stream which is rich in methane and a rich solvent bottoms stream and then recovering the lean physical solvent and a C.sub.

Abstract: A continuous process is disclosed for separating components of a hydrocarbon gas stream which are selected from the group consisting of hydrogen, nitrogen, methane, ethylene, ethane, higher saturated and unsaturated hydrocarbons, and mixtures thereof by countercurrently contacting the hydrocarbon gas stream with a physical solvent selected from the group consisting of: (1) paraffinic solvents having molecular weights ranging from 75 to 140 and UOP characterization factors ranging from 12.0 to 13.5, these factors being independent of the aromatic content of the paraffinic solvents, (2) naphthenic solvents having molecular weights ranging from 75 to 130 and UOP characterization factors ranging from 10.5 to 12.

Abstract: A gas-liquid extractive stripping process is disclosed which uses at least one preferential physical solvent in at least one solvent loop, each loop passing through at least two unit operations: extractive-stripping and distillation. At least the first extractive-stripping operation may additionally comprise a rectification section on top of the extraction section. Three products are made from streams of thermally cracked gases or refinery gases: a hydrogen-rich gas stream, a methane-rich gas stream, and a C.sub.2 =+ hydrocarbons stream which is the feed stream for the conventional fractionation train of an olefins manufacturing facility. Ethylene can be economically produced from the C.sub.2 =+ hydrocarbons product stream at a recovery of at least 99.5% and a purity of at least 99.9%.

Abstract: A continuous process for selective countercurrent extraction of C.sub.2 + hydrocarbons from a gas stream with a lean oil as solvent is rejuvenated by substitution of a preferential physical solvent for the lean oil solvent to produce a residue gas stream meeting specifications for methane content and a hydrocarbon product having a composition which can be adjusted to a selected minimum degree for ethane that is as low as 2% ethane and produce at the maximum propane content that is available from the equipment, whereby profitability of the extraction operation can be maximized at all times. The preferential physical solvent has a minimum relative volatility of methane over ethane of at least 6.0 and a solubility of at least 1.0 standard cubic foot of gaseous hydrocarbons per gallon of the solvent (thereby defining its hydrocarbon loading capacity) or, alternatively, a preferential factor of at least 6.0. Preferred solvents include polyalkylene ethers of dialkylene glycol and alkyl-substituted monocyclic C.sub.

Abstract: A process is disclosed in which a preferential physical solvent selectively extracts and strips desirable C.sub.2 + hydrocarbons from a raw hydrocarbon gas stream which is fed into the midsection of an Extractor-Stripper (ES) column, the rich solvent produced from the bottoms thereof being regenerated in a distillation column which produces a hydrocarbon gas liquid stream as product and a lean physical solvent for recycling to the top of the ES column. When certain operating conditions and product specifications necessitate operating the ES column bottoms at a temperature high enough to become relatively energy inefficient, a single-stage intermediate flashing vessel is provided for effectively removing undesirable hydrocarbons at a pressure consistent with the operating pressure of the distillation column. The separated overhead vapor stream from the flashing vessel contains all of the undesirable components along with some desirable hydrocarbons.

Abstract: A natural gas stream containing more than 3 mol percent of inert gases is extractively stripped with a preferential physical solvent to separate the inert gas from the C.sub.1 + hydrocarbons and to separate selected amounts of C.sub.2 +, C.sub.3 +, C.sub.4 +, or C.sub.5 + hydrocarbon product from a C.sub.1 gas product which may additionally contain one or more of unselected C.sub.2 -C.sub.4 hydrocarbons. The extraction and stripping are performed within at least one Extractive Stripping (ES) column which has a reboiler at its bottom, receives a stream of lean solvent at its top, and receives feed near its middle. When two ES columns are utilized, inert gas and methane may be recovered within the first ES column as overhead, and rich solvent may be withdrawn as its bottoms. The overhead may be separated in the second ES column into inert gas and methane. The rich solvent is regenerated by distilling in a product recovery column.