A method for removing contaminants from a process stream that includes the use of reticulated material to filter the process stream. The reticulated material also facilitate process stream flow distribution in process units. The reticulated material can be packed with a void space between a substantial number of the reticulated material that can be varied to enhance filtration and flow distribution. The method of filtering also provides a method of removing contaminants leaving process equipment. The methods can be used on a variety of process streams and process equipment. The reticulated material can include ceramics, metallic materials, and chemical vapor deposition elements. The reticulated material can be of various shapes and sizes, and can also be catalytically active.

Selective recovery of C2 to C4 hydrocarbons is achieved through the use of a converging-diverging nozzle, or de Laval nozzle. The vapor stream comprising C2 to C4 hydrocarbons is fed into an inlet of a de Laval nozzle having a throat. The vapor stream may have an initial temperature of between 0 C. and 100 C., and an initial pressure of between 200 psig and 500 psig. In the de Laval nozzle, the vapor stream expands after passing through the throat of the de Laval nozzle, producing a vapor stream having reduced temperature and pressure. Then, C2 to C4 hydrocarbons condense from the reduced-temperature vapor stream as liquid droplets, which may be recovered. Fractionation of C2 to C4 hydrocarbons by means of a de Laval nozzle is possible; the technique allows selective recovery of propane from a mixture of propane and ethane.

Selective recovery of C2 to C4 hydrocarbons is achieved through the use of a converging-diverging nozzle, or de Laval nozzle. The vapor stream comprising C2 to C4 hydrocarbons is fed into an inlet of a de Laval nozzle having a throat. The vapor stream may have an initial temperature of between 0 C. and 100 C., and an initial pressure of between 200 psig and 500 psig. In the de Laval nozzle, the vapor stream expands after passing through the throat of the de Laval nozzle, producing a vapor stream having reduced temperature and pressure. Then, C2 to C4 hydrocarbons condense from the reduced-temperature vapor stream as liquid droplets, which may be recovered. Fractionation of C2 to C4 hydrocarbons by means of a de Laval nozzle is possible; the technique allows selective recovery of propane from a mixture of propane and ethane.

A double liquid distribution device is suitable for a fractionating or wash column comprising a high collector tray connected to a manifold support via at least two longitudinal liquid downflow ducts. The manifold support supports at least two series of transverse tubular manifolds and feeds liquid respectively to the first series of manifolds via a first longitudinal duct and to the second series of manifolds via a second longitudinal duct. Each manifold includes distribution orifices in its under face suitable for distributing the liquid onto the top face of the packing bed. The two longitudinal liquid downflow ducts are connected together in a low portion by a communication device fitted with a valve having controlled opening suitable for allowing the liquid to be transferred between the two longitudinal ducts in controlled manner.

Systems and methods related to desalination systems are described herein. According to some embodiments, the desalination systems are transiently operated and/or configured to facilitate transient operation. In some embodiments, a liquid stream comprising water and at least one dissolved salt is circulated through a fluidic circuit comprising a desalination system. In some embodiments, a portion of the desalination system (e.g., a humidifier) is configured to remove at least a portion of the water from the liquid stream to produce a concentrated brine stream enriched in the dissolved salt. In certain cases, the concentrated brine stream is recirculated through the fluidic circuit until the concentrated brine stream reaches a relatively high density (e.g., at least about 10 pounds per gallon) and/or a relatively high salinity (e.g., a total dissolved salt concentration of at least about 25 wt %). In certain embodiments, additional salt is added to the concentrated brine stream to produce an ultra-high-density brine stream (e.g., a brine stream having a density of at least about 11.7 pounds per gallon). Some aspects relate to a system that is configured to promote energy efficiency by recovering heat from the recirculated concentrated brine stream upon discharge from the fluidic circuit.

Systems and methods related to desalination systems are described herein. According to some embodiments, the desalination systems are transiently operated and/or configured to facilitate transient operation. In some embodiments, a liquid stream comprising water and at least one dissolved salt is circulated through a fluidic circuit comprising a desalination system. In some embodiments, a portion of the desalination system (e.g., a humidifier) is configured to remove at least a portion of the water from the liquid stream to produce a concentrated brine stream enriched in the dissolved salt. In certain cases, the concentrated brine stream is recirculated through the fluidic circuit until the concentrated brine stream reaches a relatively high density (e.g., at least about 10 pounds per gallon) and/or a relatively high salinity (e.g., a total dissolved salt concentration of at least about 25 wt %). In certain embodiments, additional salt is added to the concentrated brine stream to produce an ultra-high-density brine stream (e.g., a brine stream having a density of at least about 11.7 pounds per gallon). Some aspects relate to a system that is configured to promote energy efficiency by recovering heat from the recirculated concentrated brine stream upon discharge from the fluidic circuit.

A tray for a mass-transfer column permits contact between a liquid phase and a gas phase. The tray may comprise a tray feed via which the tray is charged with the liquid phase, a tray drain via which the liquid phase drains from the tray, and first guide means for guiding the liquid phase where the first guide means forms a first course path along which the liquid phase flows from the tray feed to the tray drain, enabling contact with the gas phase. A second guide means may form a second course path overlapping with the first course path, which leads from an inlet to an outlet. The first guide means may have at least two partial concentric paths. Temperature-control fluid may flow along the second course path in at least one of the at least two partial paths opposite the flow direction of the liquid phase.

A tray for a mass-transfer column permits contact between a liquid phase and a gas phase. The tray may comprise a tray feed via which the tray is charged with the liquid phase, a tray drain via which the liquid phase drains from the tray, and first guide means for guiding the liquid phase where the first guide means forms a first course path along which the liquid phase flows from the tray feed to the tray drain, enabling contact with the gas phase. A second guide means may form a second course path overlapping with the first course path, which leads from an inlet to an outlet. The first guide means may have at least two partial concentric paths. Temperature-control fluid may flow along the second course path in at least one of the at least two partial paths opposite the flow direction of the liquid phase.

A desalination device may comprise: a membrane distillation module comprising a water feed chamber, a carrier gas (CG) chamber, and a hydrophobic microporous membrane configured to separate the water feed chamber and the CG chamber; and a bubble column dehumidifier comprising a bubble column inlet, a bubble column gas outlet, and a product outlet, wherein the MD module allows water vapor to translocate to the CG chamber, but not liquid water, and wherein the water feed each chamber has comprises a water feed inlet and a water feed outlet, wherein the CG chamber comprises a CG chamber inlet and CG chamber outlet, wherein the CG chamber outlet is upstream of and connected to the bubble column dehumidifier, and wherein the CG chamber inlet is downstream of and connected to the bubble column dehumidifier so as to cycle a carrier gas through the CG chamber and the bubble column dehumidifier.

A desalination device may comprise: a membrane distillation module comprising a water feed chamber, a carrier gas (CG) chamber, and a hydrophobic microporous membrane configured to separate the water feed chamber and the CG chamber; and a bubble column dehumidifier comprising a bubble column inlet, a bubble column gas outlet, and a product outlet, wherein the MD module allows water vapor to translocate to the CG chamber, but not liquid water, and wherein the water feed each chamber has comprises a water feed inlet and a water feed outlet, wherein the CG chamber comprises a CG chamber inlet and CG chamber outlet, wherein the CG chamber outlet is upstream of and connected to the bubble column dehumidifier, and wherein the CG chamber inlet is downstream of and connected to the bubble column dehumidifier so as to cycle a carrier gas through the CG chamber and the bubble column dehumidifier.