Abstract: The invention relates to a process and a plant for removing thiols from synthesis gas. Thiols and optionally thiophene and carbon disulfide are absorbed in a dedicated absorption stage with methanol as physical absorption medium. Methanol laden with at least thiols is freed of thiols in a stripping stage with methanol vapours as stripping gas and the methanol vapours-containing thiols are freed of methanol in a scrubbing stage. The process according to the invention minimizes methanol losses and the amounts of coolant required for the process.

Abstract: A refrigerated food pan cooling device includes a food pan receiving well and a cooling system, wherein the cooling system includes a refrigeration system with a compressor, a condenser, a metering device and an evaporator. The evaporator includes at least one first refrigerant line downstream of the metering device and upstream of the compressor. The first refrigerant line runs along an external surface of at least one of the well walls. The condenser is configured as a hot wall condenser, that lacks any fan or blower, wherein the hot wall condenser includes at least one second refrigerant line downstream of the compressor and upstream of the metering device. The second refrigerant line runs, at least partly, along an internal surface of at least the first exterior sidewall to transfer heat through the first exterior sidewall to ambient air.

Abstract: A method, system and device for recovering a desired nutrient from wastewater or digester effluents while separating the remaining components into various side streams which may have additional value or be suitable for inexpensive disposal due to the processing.

Abstract: The invention relates to various nonlimiting embodiments that include methods, apparatuses or systems for processing natural gas comprising a heavies removal column processing natural gas and light oil reflux. The overhead stream goes to heavies treated natural gas storage. The heavies removal column reboiler bottoms stream product is input to a debutanizer column. The debutanizer column overhead lights are input to a flash drum where the bottoms is pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the debutanizer reboiler bottoms product is stored as stabilized condensate. Alternatively, debutanizer column overhead lights are sent to heavies treated gas storage and the bottoms stream product goes to a depentanizer column, the overhead lights are pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the depentanizer reboiler bottoms product is stabilized condensate.

Abstract: A separation method including: an absorption process absorbing a desired component in a starting material gas into an absorption liquid by bringing the starting material gas and the absorption liquid into contact with each other inside an absorption unit; a regeneration process releasing the desired component from the absorption liquid and regenerating the absorption liquid by heating the absorption liquid, which absorbed the desired component in the absorption process, in a regeneration unit; a post-regeneration separation process separating the mixed fluid, which is the gas of the desired component released in the regeneration process and the regenerated absorption liquid, into the desired component gas and the absorption liquid; and a compression process compressing the starting material gas prior to the absorption process and the regeneration process.

Abstract: At least one gaseous impurity, for example silane, is removed by absorption from a feed gas stream, for example a gas stream comprising nitrogen and hydrogen, the gaseous impurity being less volatile than the feed gas stream. The absorption is effected by a sub-cooled absorbent at a first cryogenic temperature and a first pressure. The absorbent is typically propane. The absorption may be conducted in a liquid-vapor contact column (130). Absorbent containing impurity may be regenerated in a regeneration vessel 150 and returned to the column (130).

Abstract: A process for removing carbon dioxide from a carbon dioxide-loaded solvent uses two stages of flash apparatus. Carbon dioxide is flashed from the solvent at a higher temperature and pressure in the first stage, and a lower temperature and pressure in the second stage, and is fed to a multi-stage compression train for high pressure liquefaction. Because some of the carbon dioxide fed to the compression train is already under pressure, less energy is required to further compress the carbon dioxide to a liquid state, compared to conventional processes.

Abstract: A distillation apparatus includes: a distillation column group in which a plurality of distillation columns, which are respectively equipped with a reboiler, is connected in the form of a distillation cascade; feed-gas condensers which liquefy feed gases from respective former distillation columns and feed said liquefied feed gases to respective latter distillation columns; gas-feeding lines which connect the respective former distillation columns and the respective feed-gas condensers; and liquid-feeding lines which connect the respective feed-gas condensers and the respective latter distillation columns.

Abstract: A process for separating carbon dioxide from a carbon dioxide containing fluid comprises the steps of: compressing the fluid in a compressor to form a compressed fluid, drying at least part of the compressed fluid to form a compressed and dried fluid, cooling at least part of the compressed and dried fluid to form a compressed, dried and cooled fluid, separating the compressed, dried and cooled fluid at a temperature lower than 0° C. into a carbon dioxide rich stream, a carbon dioxide lean stream and at least one intermediate purity liquid stream having a carbon dioxide purity lower than that of the carbon dioxide rich stream and higher than that of the carbon dioxide lean stream, expanding at least one intermediate purity liquid stream to produce at least one expanded stream using at least one expanded stream to cool the compressed and dried fluid and recycling at least part of the expanded stream.

Abstract: Methods and systems are provided for treating hydrogen sulfide rich sour gas through a series of fractionation columns. The processes disclosed herein and the variations thereof provide optimized processes for the removal of hydrogen sulfide from sour gas through the introduction of innovative azeotrope breakers, novel configurations of process equipment, and optimized operating conditions. Advantages of certain embodiments of the present invention include reduced equipment requirements, improved process efficiencies, reduced operating costs, and reduced capital costs. Other advantages include better process suitability to certain environmental conditions such as the arctic cold when compared to conventional amine treatment processes.

Abstract: A method for selective extraction of natural gas liquids from “rich” natural gas. The method involves interacting a rich natural gas stream with Liquid Natural Gas (LNG) by mixing Liquid Natural Gas into the rich natural gas stream to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point, whereby a selected hydrocarbon liquid carried in the rich natural gas stream is condensed.

Abstract: A semi-closed loop system for producing liquefied natural gas (LNG) that combines certain advantages of closed-loop systems with certain advantages of open-loop systems to provide a more efficient and effective hybrid system. In the semi-closed loop system, the final methane refrigeration cycle provides significant cooling of the natural gas stream via indirect heat transfer, as opposed to expansion-type cooling. A minor portion of the LNG product from the methane refrigeration cycle is used as make-up refrigerant in the methane refrigeration cycle. A pressurized portion of the refrigerant from the methane refrigeration cycle is employed as fuel gas. Excess refrigerant from the methane refrigeration cycle can be recombined with the processed natural gas stream, rather than flared.

Abstract: Contemplated methods and configurations use a cooled ethane and CO2-containing feed gas that is expanded in a first turbo-expander and subsequently heat-exchanged to allow for relatively high expander inlet temperatures to a second turbo expander. Consequently, the relatively warm demethanizer feed from the second expander effectively removes CO2 from the ethane product and prevents carbon dioxide freezing in the demethanizer, while another portion of the heat-exchanged and expanded feed gas is further chilled and reduced in pressure to form a lean reflux for high ethane recovery.

Abstract: A fan integrated thermal management device, such as a heat sink, may include an integrated fan to facilitate air flow through the device. One embodiment of the thermal management device may include a heat-conductive base and a plurality of heat-conductive extensions extending from the base and defining one or more fan blade regions. One or more fans may be mounted relative to the heat-conductive extensions such that at least one fan blade is located in the fan blade region and is configured to rotate through the fan blade region. Of course, many alternatives, variations, and modifications are possible without departing from this embodiment.

Abstract: An NGL recovery plant includes a demethanizer (7) in which internally generated and subcooled lean oil absorbs CO2 and C2 from a gas stream (11), thereby preventing build-up and freezing problems associated with CO2, especially where the feed gas has a CO2 treatment at ethane recoveries above 90% and propane recoveries of at least 99%.

Abstract: A cryogenic process for the production of oxygen by cryogenic distillation using an air separation unit comprising a double column, said double column comprising a high pressure column and a low pressure column comprising the steps of: sending compressed, cooled and purified air to the high pressure column in gaseous form, sending oxygen enriched fluid from the bottom of the high pressure column to the low pressure column, removing nitrogen enriched gas from the top of the high pressure column, sending a first portion of nitrogen enriched gas to a lower reboiler in the low pressure column following compression in a cold compressor having a cryogenic inlet temperature, sending a second portion of nitrogen enriched gas to an upper reboiler in the low pressure column, sending nitrogen enriched liquid from at least one of the first and second reboilers to at least one of the high pressure column and the low pressure column, expanding a stream of nitrogen enriched gas from the high pressure column in an expander f

Abstract: A process for separating the components of a multi-component gas stream is disclosed. The multi-component gas stream is contacted with a solvent in an extractor at cryogenic temperatures to produce an overhead stream enriched with unabsorbed component(s) and a rich solvent bottoms stream enriched with absorbed component(s). The rich solvent bottoms stream is then flash evaporated to regenerate the lean solvent and to recover the absorbed component(s) as an overhead stream, which is compressed to produce a product stream. The regenerated solvent is recycled to the extractor.

Abstract: A process for the recovery of high purity hydrogen for recycling to a hydroprocessing or similar unit located in an integrated refinery facility includes sampling and providing analytical information on the make-up of the hydrogen-containing feedstream entering the bottom of a stripping column and the composition of the hydrogen recycle stream at, and/or approaching the top of the stripping column to a computer-directed control system in real time for the purpose of controlling the selection and the volumetric flow rate of one or more “refinery solvents” into the column to maximize the removal of non-hydrogen gases from the feedstream and to thereby maximize the percentage of hydrogen in the recycle gas stream.

Abstract: A process and apparatus for the recovery of ethane and heavier components from a hydrocarbon feed gas stream. Feed gas stream is cooled and separated into a vapor stream and a condensed stream. Vapor stream is divided into a first and a second gas streams. First gas stream is expanded and sent to a fractionation tower. Second gas stream is supplied to an absorber tower. At least a part of the first liquid stream is cooled and sent to the absorber. Absorber column produces a lean vapor stream and a second condensed stream. Lean vapor stream is cooled and sent to the fractionation tower. Second condensed stream is subcooled and supplied to the fractionation tower. Temperatures and pressures of the streams and columns are maintained to recover a major portion of ethane and heavier hydrocarbon components as bottom product, and produce at the fractionation tower overhead, a residue gas stream.

Abstract: A portable, potable-water generator for producing high-purity liquid water by condensation of water vapor from ambient air. The generator (125) employs an air filter (119) to remove particulates and aerosols from the incoming air. An enclosed heat absorber cools the filtered air to its dew point and collects droplets of condensate into a condensate collector (5). Before discharge, the collected dew is treated in a bacteriostat loop to destroy adventitious living organisms and to filter out undesirable and dangerous contaminants. A recirculation loop provides the ability to recirculate stored condensate, including during periods of inactivity. Further, quick disconnect fittings (55b) and variable length flexible tubing allows use of the invention to serve remote dispensers and/or appliances and allow use of municipal water treated through the apparatus in low condensate situations.

Abstract: A gas processing plant has a de-ethanizer and a refluxed absorber, wherein the absorber operates at higher pressure than the de-ethanizer, and wherein at least a portion of the absorber bottoms product is expanded to provide cooling for the absorber reflux stream and/or the distillation column feed stream. Especially contemplated gas processing plants include propane and ethane recovery plants, and where the gas processing plant is an ethane recovery plant, it is contemplated that the ethane product comprises no more than 500 ppm carbon dioxide.

Abstract: A process for recovering hydrogen from a stream comprised of hydrogen, non-condensable gases, and propane and lighter hydrocarbons, wherein the process comprises the steps of stripping hydrogen and non condensable gases out of the feed light ends stream with methane vapor, washing the stripped hydrogen stream with liquid methane to absorb the non condensable gases, and washing the hydrogen stream with a hydrocarbon lean oil such as liquid ethane to absorb methane, to produce the product hydrogen stream.

Abstract: The natural gas is successively contacted in column CA with a relatively methanol-rich solvent flowing in through line 4, then with a relatively poor solvent flowing in through line 9. The acid gas-containing solvent recovered through line 3 at the bottom of column CA is expanded through valves V1 and V2 to release acid gases through line 6. A fraction of the expanded solvent is distilled in column CR. The regenerated solvent obtained at the bottom of column CR is sent to the top of column CA through line 9. A second fraction of the expanded solvent is mixed with a solvent drawn off from column CR at an intermediate point between the bottom and the top of this column. This mixture of solvents is sent through line 4 into column CA.

Abstract: A gas processing plant has a de-ethanizer (106) and a refluxed absorber (103), wherein the absorber (103) operates at higher pressure than the de-ethanizer (106), and wherein at least a portion of the absorber bottoms product (7) is expanded to provide cooling for the absorber reflux stream and/or the distillation column feed stream. Especially contemplated gas processing plants include propane and ethane recovery plants, and where the gas processing plant is an ethane recovery plant, it is contemplated that the ethane product comprises no more than 500 ppm carbon dioxide.

Abstract: A process and apparatus to increase the recovery of ethane, propane, and heavier compounds from a hydrocarbon gas stream is provided. The process can be configured to recover ethane and heavier compounds or propane and heavier compounds, depending upon the market conditions. The process utilizes an additional reflux stream to the absorber column that is lean in ethane and propane compared to the deethanizer overhead. The additional reflux stream is taken as a side stream of the residue gas stream that is cooled, condensed, and then fed at the top of the absorber to enhanced C3+ recovery. The additional lean reflux stream can also be taken as a side stream of the first vapor stream from the cold separator.

Abstract: Nitrogen is rejected from a pressurised feed gas stream comprising methane and nitrogen by cooling the feed gas stream in a main heat exchanger 10 and rectifying the cooled feed gas stream in a double rectification column 20 comprising a higher pressure rectification column 22, a lower pressure rectification column 24, and a condenser-reboiler 25 placing the higher pressure column 22 in heat exchange relationship with the lower pressure column 24. A pump 50 withdraws a methane product stream from the column 24. The methane product stream is pressurised by the pump 50 and is vaporised in the main heat exchanger 10. The pressurised feed gas stream is expanded with the performance of external work in an expansion turbine 6 upstream of the main heat exchanger 10.

Abstract: Process for pretreating a natural gas under pressure containing hydrocarbons, acid compounds such as hydrogen sulfide and carbon dioxide, and water. The natural gas is cooled to condense part of the water. The partially dehydrated natural gas is then contacted with a liquid stream consisting of a majority of hydrogen in two successive contact zones so as to obtain a natural gas containing substantially no water any more. Finally, this dehydrated natural gas is cooled to condense and separate the acid compounds, this cooling stage being carried out by means of a heat exchanger, an expander or a venturi neck.

Abstract: Various methods and apparatus for maximizing the efficiency of hydrate-based desalination or other water purification in open-water or partially open-water installations are disclosed. In one embodiment, water is accessed from depth where the ambient temperature is as cold as possible, which depth is other than the maximum depth of the hydrate fractionation column used in the process. The accessed water preferably is brought to reduced pressures so that gases other than hydrate-forming gases that are dissolved in the water to be treated are exsolved. Using pre-pressurized sources of hydrate-forming substances, including deep-sea natural gas deposits or supplies of liquified natural gas being transported by sea, are also disclosed. A multiple column, detachable column fractionation installation is disclosed, as is a hybrid installation having an underwater hydrate formation portion and a land-based dissociation and heat-exchange section.

Abstract: A technique is set forth to reduce the heat requirement of conventional distillation processes which separate feed mixtures containing three or more components. The technique provides a great deal of flexibility in adjusting the temperatures of the required utilities including a scenario where the heat requirement is reduced without a need for additional higher temperature (and more costly) heat utility. In this technique, when a liquid bottoms stream (or gaseous overhead stream) containing two or more components is sent from an earlier column to a subsequent column, then a return vapor (or liquid) stream is implemented between the same locations in the two columns.

Abstract: A process for separation of gases into two components of different boiling points, for example in the separation of ethane from natural gas, comprises a first separation tower V1 and a second separation tower V2. Liquid in stream 5 from a bottom of the first tower is expanded and cooled and is then communicated in stream 6 to the second tower at a lower pressure. Gas from the second tower is communicated back to the first tower so that the first component in stream 10 is extracted from the top of the first tower and the second component in stream 11 is extracted from the bottom of the second tower. A third tower V3 acts as a recycle fractionator upon the gas in stream 7 extracted from the top of the second tower with that gas being compressed into the third tower which is at high pressure.

Abstract: Process for treating a gas comprising one or more constituents to be separated, wherein the gas to be processed (G) is mixed at least partly with a solvent S selected to selectively retain at least part of the gas constituents to be separated, the mixture of gas (G) and of solvent (S) is cooled by circulating in at least one heat exchange zone so as to obtain, at the outlet of said heat exchange zone, at least a gas phase (G.sub.1) depleted in at least one of the constituents to be separated and a solvent phase (S.sub.1) enriched in said constituents, said enriched solvent phase (S.sub.1) is separated from said gas phase (G.sub.1) and it is recycled to the heat exchange zone in order to cool said gas-solvent mixture (stage b), said solvent phase (S.sub.1) consisting, at the outlet of the heat exchange zone, of at least a gas phase (G.sub.2) enriched in the constituents to be separated and of a liquid solvent phase (S), the gas phase (G.sub.

Abstract: Method for the liquefaction of a hydrocarbon-rich gas stream containing aromatic and heavy hydrocarbons, in particular a natural gas stream, where, prior to the liquefaction, a separation of the aromatic and the heavy hydrocarbons, in particular the C.sub.5+ hydrocarbons, comprisesa) a fraction (9, 11, 14) containing heavy hydrocarbons is admixed to the hydrocarbon-rich gas stream (1) to be liquefied,b) this mixed fraction (1, 2) is supplied to a separator (D),c) a gas fraction (3) freed of aromatic and heavy hydrocarbons is withdrawn from separator (D) and liquefied (E2), andd) a liquid fraction (5) enriched with aromatic and heavy hydrocarbons is withdrawn from separator (D).

Abstract: A process for the dehydration, deacidification and stripping of a gas, characterized in that:(a) at least one fraction of the gas is contacted with an aqueous phase containing methanol, the resultant gas being thus charged with methanol being withdrawn from stage (a);(b) the gas withdrawn from stage (a) is contacted with a mixture of solvents comprising methanol, water, and a solvent heavier than methanol, the gas leaving stage (b) being thus at least in part freed of the acid gases which it contained initially;(c) the mixture of solvent obtained from stage (b) is at least in part generated by special reduction and/or heating while liberating at least part of the acid gases, the mixture of solvent being at least partially regenerated, or being at the outlet of stage (c) recycled through stage (b); and(d) the gas obtained from (stage b) is refrigerated while producing at least an aqueous phase containing methanol which is at least in part recycled through stage (a).

Abstract: The present invention is a plurality of stages for partial condensation and phase separation a process gas stream, preferably containing substantial amounts of light olefins, methane, and hydrogen, but containing initially at least substantial amounts of methane and ethylene. Each condensation and separation stage is refrigerated with a subcooled and flashed high pressure liquid of a mixed refrigerant refrigeration loop, wherein throughout the loop the relative component ratios of the mixed refrigerant components are constant, contrasted with the several mixed refrigerant processes of the prior art where for all the streams of each closed refrigeration loop. In addition, rectification and/or stripping sections of an ethylene separation train have a common support construction taking advantage of relatively similar column diameters to reduce the total number of columns in the process.

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: Increased recovery of propane, butane and other heavier components found in a natural gas stream is achieved by installing an absorber upstream from an expander and a separator. The separator is downstream from the expander and returns the liquid stream generated by the separator back to the absorber. Additionally, the recovery of propane, butane and other heavier components is enhanced by combining the upper gas stream from a distillation column with the upper gas stream from the absorber prior to injecting this combination into the separator. The upper gas stream removed from the separator is then subsequently processed for the recovery of a predominately methane and ethane gas stream while the bottom liquid stream from the absorber is subsequently distilled for the generation of a stream consisting predominately of propane, butane and other heavy hydrocarbon components. Alternate embodiments include an additional reflux separator in the system, or substitution of an additional absorber for the separator.

Abstract: A method of separating from gaseous media, such as air or technical gases, organic vapors by substantially isothermally raising the pressure of the media and subjecting them to cooling in a cold scrubber receiving its operating low temperature from circulating first and second flows of refrigerants of moderate and significant refrigeration parameters and provided by resulting condensates.

Abstract: A retrofitted 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.