Embodiments of the disclosure provide a system and method for producing a linear alpha olefin. A disulfide, a hydrogen donating compound, and water are combined to produce a mixture. The mixture is introduced to a reactor operated at a pressure equal to or greater than 22.06 MPa and a temperature equal to or greater than 374 deg. C. to produce an effluent stream. The effluent stream is separated to produce a product stream including the linear alpha olefin. The disulfide can be a compound of formula R—S—S—R′ where R is a first alkyl group having carbon atoms ranging from 1 to 12 and R′ is a second alkyl group having carbon atoms ranging from 5 to 12. The hydrogen donating compound can include a partially hydrogenated multi-ring aromatic compound.

A process for producing bis(fluorosulfonyl) imide includes providing a solution comprising fluorosulfonic acid and urea, the solution maintained at a solution temperature from about 0° C. to about 70° C.; reacting the solution in the presence of a reaction medium at a reaction temperature from 80° C. to about 170° C. to produce a product stream including bis(fluorosulfonyl) imide, ammonium fluorosulfate and the reaction medium; separating the ammonium fluorosulfate from the product stream to produce an intermediate product stream; and separating the intermediate product stream into a concentrated product stream and a first recycle stream, the concentrated product stream including a higher concentration of bis(fluorosulfonyl) imide than the first recycle stream.

A plant for producing a synthesis gas chiefly consisting of hydrogen and carbon monoxide by catalytic steam reformation of a hydrocarbonaceous feed gas, wherein the heat of burners required for the chemical reforming reactions to take place is generated by producing a flue gas and wherein, by utilizing the heat contained in the synthesis gas and in the flue gas, a pure steam is generated from boiler feed water and a process steam is generated from process condensate, wherein for the generation of the pure steam synthesis gas and flue gas are used and for the generation of the process steam a part of the pure steam is used as heat-transfer medium and the remaining part of the pure steam is discharged from the process as export steam.

The invention discloses a method for producing bio-fuel (BF) from a high-viscosity biomass using thermo-chemical conversion of the biomass in a production line (10) with pumping means (PM), heating means (HM) and cooling means (CM). The method has the steps of 1) operating the pumping means, the heating means and the cooling means so that the production line is under supercritical fluid conditions (SCF) to induce biomass conversion in a conversion zone (CZ) within the production line, and 2) operating the pumping means so that at least part of the production line is in an oscillatory flow (OF) mode. The invention is advantageous for providing an improved method for producing biofuel from a high-viscosity biomass. This is performed by an advantageous combination of two operating modes: supercritical fluid (SCF) conditions and oscillatory flow (OF).

A reactor and process for the production of bio-diesel. The reactor includes one or more coiled reaction lines. The lines are positioned within a tank containing a heat transfer media such as molten salt, maintained at about 750° F. A pump circulates the media within the tank. An emulsion of alcohol; refined feed stock, including glycerides and/or fatty acids; and preferably water is pumped through the reaction lines at temperatures and pressures sufficient to maintain the alcohol in a super-critical state. The curvature of the coils, pump pulsing, and the flow rate of the emulsion keep the emulsion in a turbulent state while in the reactor, ensuring thorough mixing of the alcohol and feed stock. The alcohol reacts with the glycerides and fatty acids to form bio-diesel. The reaction is fast, efficient with regard to energy input and waste generation, and requires minimal alcohol.

A system and method for producing an aerogel composite material includes a reaction vessel having a movable carrier basket for receiving a plurality of fiber mats, and a plurality of plates to space the fiber mats apart from one another. Once the plates have been removed, there are gaps between the aerogel insulating boards, through which hot drying air can be blown during a drying process. The method has the advantage that the quantities of solvents and reagents to be disposed of are minimal, and in addition thereto, no complex work-up processes are necessary.

The invention relates to a process for the oligomerization of ethylene, carried out at a pressure of between 0.1 and 10.0 MPa, at a temperature of between 30 and 200° C., in a cascade of N gas/liquid reactors in series, N being at least equal to 2, comprising a step of introducing a catalytic oligomerization system into at least the first reactor of the cascade, a step of bringing said catalytic system and an optional solvent into contact with ethylene by introducing said ethylene into the lower part of the reaction chamber of at least the first reactor of the cascade, for each reactor n, a step of withdrawing a liquid fraction in the lower part of the reaction chamber of the reactor n, the liquid fraction being separated into two streams: a first stream corresponding to a first, “main”, part of the liquid fraction, which is conveyed to a heat exchanger for cooling; a second stream corresponding to the second part of the liquid fraction which constitutes the liquid feedstock of the following reactor n+1 in the cascade, a step of introducing said second part of the liquid phase withdrawn from the reactor n towards the reaction chamber of the following reactor n+1 in the direction of flow, a step of cooling said first part of the liquid fraction withdrawn from the reactor n in step c) by passing said first part of the liquid fraction into a heat exchanger in order to obtain a cooled liquid fraction, a step of introducing said liquid fraction cooled in step e) at the top of the reaction chamber of said reactor n, the steps a) to f) being carried out, unless indicated otherwise, for each reactor n of the cascade, n being between 1 and N. The invention also relates to a device of N stirred gas/liquid reactors in a cascade, enabling the oligomerization process to be carried out.

A device for converting cellulose to sugar comprises a reactor chamber with a plurality of control components, and a control assembly. The control assembly is operatively connected to the reactor chamber, a drive assembly and control components to transmit and receive interoperability signals. The device has an inlet hopper with a detector, a crusher, an outlet hopper, a sensor assembly, a steam inlet, and a carbon dioxide inlet. The inlet hopper is configured to receive and analyze proportion data of matters in a feedstock and catalyst mixture via the detector. The crusher receives and grinds the mixture from the inlet hopper to induce chemical reaction for producing sugar. The outlet hopper is configured to determine a proportion data of matter in the grinded mixture. The control assembly is configured to determine adjustments need to be performed on the components and drive assembly to optimize the sugar production.

The present invention relates to hydroformylation reaction processes. In one aspect, a hydroformylation reaction process comprises (a) contacting an olefin, hydrogen, and carbon monoxide in the presence of a homogeneous catalyst in a reactor to provide a reaction fluid, wherein the reactor comprises one or more reaction zones; (b) removing a portion of the reaction fluid from a first reaction zone; (c) passing at least a portion of the removed reaction fluid through a shear mixing apparatus to produce bubbles in the portion of the removed reaction fluid, wherein at least a portion of hydrogen and carbon monoxide provided to the reactor is introduced through the shear mixing apparatus; and (d) returning the removed reaction fluid to the first reaction zone through one or more nozzles wherein the returning reaction fluid exiting each nozzle is a jet, wherein the mixing energy density provided to the reactor by the jets is greater than or equal to 500 Watts/m.sup.3.

A pressurized carbonation reaction apparatus and method thereof are provided. The apparatus comprises: an atomizing gas tank, a plurality of compressors, a plurality of buffer tanks, a plurality of pre-heaters, a pressurized liquid tank, a nozzle, a raw material tank, a carbon dioxide tank, a high-pressure reactor, a raw product tank, a feed pump, a plurality of pressure display gauges, a plurality of temperature controllers with display gauges and a plurality of back pressure valves. The method comprises: dissolving a solid material in a solvent, and storing a resulting liquid material in the raw material tank; introducing gas in the carbon dioxide tank to the high-pressure reactor, controlling temperatures of the high-pressure reactor and the pressurized liquid tank, and pumping, by the feed pump, the liquid material into the pressurized liquid tank to ensure a pressure difference between the pressurized liquid tank and the high-pressure reactor; opening a second check valve, and ensuring that the liquid material reacts with a carbon dioxide atmosphere in the high-pressure reactor after being atomized via the nozzle under a stable pressure difference between the high-pressure reactor and the pressurized liquid tank; and ensuring that when the liquid material in the high-pressure reactor is at a corresponding liquid level, a fifth check valve is opened and discharge continues to obtain a reaction product.