A method of upgrading an overflash stream from a vacuum distillation unit comprising the steps of separating the overflash stream from an atmospheric residue stream, the overflash stream comprises an overflash fraction having a T10% between 475 and 530° C. and a T90% between 600 and 700° C.; introducing the reactor feed to a supercritical reactor at a temperature between 380° C. and 500° C. and a pressure between 25 MPa and 30 MPa; maintaining upgrading reactions in the supercritical reactor to upgrade the overflash fraction such that a reactor effluent comprises upgraded hydrocarbons relative to the overflash fraction; reducing a temperature of a reactor effluent in a cooling device to produce a cooled stream; reducing a pressure of the cooled stream in a depressurizing device to produce a discharged stream; and separating the discharged stream in a gas-liquid separator to produce a liquid phase product.

Provided are a vacuum rectification tower with a satellite-type tower kettle and a vacuum rectification method for atmospheric pressure residual oil. The vacuum rectification tower includes a satellite-surrounded vacuum tower kettle and a rectifying section; the satellite-surrounded vacuum tower kettle includes a main tower kettle and a plurality of sub-reactors arranged outside the main tower kettle in a satellite-surrounded mode; the main tower kettle is provided with a first outlet and a plurality of spray inlets, and a top portion of the main tower kettle has an opening; the sub-reactor is provided with a second outlet and a first inlet, the spray inlets are connected with the second outlets of each sub-reactor in a one-to-one correspondence, and the first outlet is connected with the first inlets. The above vacuum rectification tower is used for treating the atmospheric pressure residual oil, and an extraction rate of light oil may be effectively improved under relatively mild temperature and pressure environment.

The present invention relates to a process for distillative purification of a crude isocyanate obtained by phosgenation of the corresponding amine in a distillation apparatus under vacuum to obtain the corresponding isocyanate, characterized in that at least one liquid ring compressor is used to generate the vacuum in the distillation apparatus, a particular operating liquid is used for the at least one liquid ring compressor, the pressure p on the suction side of the at least one liquid ring compressor is 10 to 200 mbar(a), the operating temperature of the at least one liquid ring compressor is −17° C. to +15° C. and the operating liquid at the exit from the at least one liquid ring compressor has an AC value of less than 35 000 ppm, to a corresponding use of at least one liquid ring compressor for generating a vacuum in an apparatus for distillation of a crude isocyanate and to a corresponding process for operating a liquid ring compressor for providing the vacuum for distillative purification of an isocyanate obtained by phosgenation of the corresponding amine in a distillation apparatus to obtain the corresponding isocyanate.

An oil dehydrator, comprising; a vacuum chamber, a vacuum pump arranged at an upper end region of the vacuum chamber for establishing a negative pressure within the vacuum chamber and for fluid transportation of water and air out from the vacuum chamber through an outlet opening, and a pipe for fluid transportation of oil into and/or out from the vacuum chamber, where the pipe is connected to a lower end region of the vacuum chamber, wherein the vacuum chamber at the lower end region has at least one flow channel fluidly connecting the vacuum chamber and the pipe, wherein an orifice check valve is arranged between the vacuum chamber and the pipe for controlling the flow of oil into and out from the vacuum chamber through the at least one flow channel.

An evaporator for submerged combustion and delayed evaporation, a method of the same and a system of combined evaporation devices, the evaporator for submerged combustion and delayed evaporation comprises: a housing formed with a space for containing an evaporating liquid; a separator plate arranged in an interior of the housing and dividing the housing into a heat transfer (submerged combustion) area and an evaporation area; a vapor chamber located above a liquid surface of the evaporation area; a flue gas chamber located above a liquid surface of the heat transfer area, wherein the flue gas chamber is provided with a flue gas outlet, the flue gas outlet is provided with a pressure valve which is capable of controlling a gas pressure within the flue gas chamber such that a gas pressure within the flue gas chamber is larger than a gas pressure within the vapor chamber.

A remediation plant for remediating drilling mud, cuttings, and fluids. The preferred plant includes a reboiler that is adapted to provide heat to the drilling mud, cuttings, and fluid, a mud drum that is operatively connected to the reboiler, a distillation column that is operatively connected to the reboiler, a heat exchanger that is operatively connected to the reboiler, a condenser that is operatively connected to the distillation column, a condenser tank that is operatively connected to the condenser, an oil-water separator that is operatively connected to the condenser tank, and a pump that is operatively connected to the oil-water separator. The preferred remediation plant is adapted to remove synthetic drilling fluid from drilling mud, cuttings, and fluids. A method for remediating drilling mud, cuttings, and fluid.

A method for recovering CO.sub.2 in the Rectisol process. The method includes at least the following steps: performing reduced-pressure flash distillation treatment on the CO.sub.2-rich methanol liquid, and outputing the CO.sub.2 desorbed gas obtained after the reduced-pressure flash distillation treatment as a product gas; performing heat exchange flash distillation treatment on a first methanol treatment liquid obtained after the reduced-pressure flash distillation treatment, and outputing the CO.sub.2 desorbed gas obtained after the heat exchange flash distillation treatment as a product gas; performing vacuum flash distillation treatment on a second methanol treatment liquid obtained after the heat exchange flash distillation treatment, and outputing the CO.sub.2 desorbed gas obtained after the vacuum flash distillation treatment as a product gas. Reduced-pressure flash distillation treatment, heat exchange flash distillation treatment and vacuum flash distillation treatment are sequentially performed on the CO.sub.2-rich methanol liquid in this method.

A purification system for nitrogen gas and xenon gas in water and a static isotopic analysis method thereof are provided. The system includes a sample container, a carbon dioxide ice cold trap, a gas delivery main pipe and a mass spectrometer for noble gas communicated sequentially. The gas delivery main pipe is provided with branch pipelines communicated with a cryo pump and a vacuum pump set respectively, the mass spectrometer for noble gas is communicated with the vacuum pump set, and the cryo pump adsorbs or releases nitrogen gas and/or xenon gas by setting different temperatures of the cryo pump. Inlet and outlet sides of the carbon dioxide ice cold trap are respectively provided with a first valve and a second valve. Fourth and fifth valves are respectively disposed between the gas delivery main pipe and the vacuum pump set, and between the gas delivery main pipe and the cryo pump.

A metal surface treatment liquid recycling system includes a treatment liquid collecting tank, a pre-treatment device, a nanofiltration device and a vacuum distillation device, all of which are connected sequentially. The nanofiltration device includes a feed tank, a first-stage nanofiltration membrane unit, and a second-stage nanofiltration membrane unit. Treatment wastewater in the treatment liquid collecting tank is fed into the pre-treatment device to filter out suspended solids and then enter the feed tank. The wastewater in the feed tank is filtered by the first-stage nanofiltration membrane unit and transformed to a first-stage concentrated waste liquid and first-stage infiltration fluids. The first-stage infiltration fluids are fed into and re-filtered by the second-stage nanofiltration membrane unit and transformed to a second-stage concentrated waste liquid and second-stage infiltration fluids. The second-stage infiltration fluids are evaporated and concentrated by the vacuum distillation device for generation of distilled water and high-concentration acid concentrated fluids.

A method for separating a lubrication oil from a waste fluid includes separating water from the waste fluid by heating the waste fluid while sealed in a first vacuum chamber to a first temperature and first pressure. Fuel oil is separated from a fluid received from the first vacuum chamber by heating the fluid while sealed in a second vacuum chamber to a second temperature that is higher than the first temperature and at a second pressure. Finally, the lubrication oil is separated from a fluid received from the second vacuum chamber by heating the fluid received from the second vacuum chamber while sealed in a third vacuum chamber to a third temperature that is higher than the second temperature and at a third pressure.