A counter-flow simultaneous heat and mass exchange device is operated by directing flows of two fluids into a heat and mass exchange device at initial mass flow rates where ideal changes in total enthalpy rates of the two fluids are unequal. At least one of the following state variables in the fluids is measured: temperature, pressure and concentration, which together define the thermodynamic state of the two fluid streams at the points of entry to and exit from the device. The mass flow rate of at least one of the two fluids is changed such that the ideal change in total enthalpy rates of the two fluids through the device are brought closer to being equal.

A distillation column and tray assembly is disclosed herein. The distillation column includes a removable inner tray assembly with adjustable downcomer tubes. The removable tray assembly enables the user to selectively change distillation plates when so removed. When removed, a distiller or brewer may adjust the downcomer tubes to change the fluid level on the distillation plates, or bypass certain distillation plates completely. Certain embodiments of the invention include a feature of an O-ring recessed around a perimeter of the plates permitting a tight seal and reducing manufacturing costs.

The invention relates to a gas/liquid separation column extending mainly along a vertical axis and comprising an external wall delimiting an internal space in which are arranged at least one first contact member in which the liquid and the gas are brought into contact and at least one dispensing device configured to collect the liquid resulting from the first contact member and to distribute it to a second contact member. At least one box for separating a two-phase fluid is arranged in the internal space of the column between the first contact member and the dispensing device against the wall of the column fed by a duct which passes through a wall of the separation box.

The invention relates to a gas/liquid separation column extending mainly along a vertical axis and comprising an external wall delimiting an internal space in which are arranged at least one first contact member in which the liquid and the gas are brought into contact and at least one dispensing device configured to collect the liquid resulting from the first contact member and to distribute it to a second contact member. At least one box for separating a two-phase fluid is arranged in the internal space of the column between the first contact member and the dispensing device against the wall of the column fed by a duct which passes through a wall of the separation box.

The use transmission/absorbance of visible light to determine accurate separation of distillation products emerging from a condenser is described. Changes in wavelength and intensity of light transmitted through or absorbed by the distillate, post condenser, determine when a new fraction passes through the condenser, and may be directed to an appropriate collection vessel.

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 re-duced 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 select-ive 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 re-duced 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 select-ive recovery of propane from a mixture of propane and ethane.

Provided is a separation device, including: a gas-liquid contact flow passage having a distillate discharge port formed on one end side and a bottom product discharge port formed on another end side; a raw material liquid introduction port formed between the distillate discharge port and the bottom product discharge port in the gas-liquid contact flow passage; a stripping section, which is provided between the raw material liquid introduction port and the bottom product discharge port and is configured to heat a liquid in the gas-liquid contact flow passage; a rectification section, which is provided between the raw material liquid introduction port and the distillate discharge port and is configured to cool a gas in the gas-liquid contact flow passage; and a porous body arranged in the gas-liquid contact flow passage.

A vapor-liquid contact tray apparatus includes a tray having a plurality of apertures for passage of fluid through the tray. The apertures are arranged in a first group of three adjacent rows extending substantially parallel to a main liquid flow path of the tray. Apertures of the middle row are offset along the main liquid flow path on the tray from adjacent apertures of the other two rows to form a triangular pattern of adjacent apertures across the three adjacent rows. The apertures have a length and a width, each length is oriented substantially parallel to its row and each width is oriented substantially perpendicular to its row. Centers of adjacent apertures within each row are separated by a first spacing which is equal to or between 2.5 and 4.5 times the average length of the apertures in that row. Adjacent rows are separated by a second spacing which is equal to or between 1.5 and 2.5 times the average width of the apertures of the adjacent rows.

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.