A process for continuous preparation of halogenated alkoxyethane of general formula XClHC—CF.sub.2OR, where X is —Cl or -f and OR is C.sub.1-4 alkoxy, the process comprising a step of introducing in a flow reactor reaction components comprising (i) a compound of general formula XClHC—CYF.sub.2, where each of X and Y is independently —Cl or —F, (ii) a base, and (iii) a C.sub.1-4 alkanol, wherein a) the flow reactor comprises one or more tubular flow line(s) through which the reaction components flow as a reaction mixture, c) the halogenated alkoxyethane is formed at least upon the reaction components mixing, with the so formed halogenated alkoxyethane flowing out of the flow reactor in a reactor effluent, and b) the base is one that forms a salt soluble in the alkanol during formation of the halogenated alkoxyethane.

Described herein are thermal condensation reactors and processes of using the same. A presently described thermal condensation reactor includes a heat transfer chamber, wherein the heat transfer chamber is a fluidized bed having a fluidization gas flow in a first direction, and wherein the heat transfer chamber has a plurality of heating zones that may be maintained at different temperatures, and a plurality of reaction tubes disposed in the heat transfer chamber in a second direction perpendicular to the fluidization gas flow, each reaction tube having a reactant gas flow that passes through the plurality of heating zones.

A process for a continuous condensation reaction with feedstocks derived from bio-renewable resources, e.g., pine chemical derived feedstock, is disclosed. The process employs at least a multi-stage mixing reactor, selected from any of a multi-stage continuous stirred tank reactor (CSTR), a multi-stage horizontal continuous stirred tank reactor (HCSTR), or a continuous oscillating baffle reactor (COBR). The multi-stage mixing reactors are provided with a plurality of baffles for creating a mixing in a number of stages or cells created by the baffles, allowing the condensation reaction to proceed at a production rate at least twice that of a batch process with reactors of equivalent volume. The feedstocks derived from bio-renewable resources is selected from gum rosin, wood rosin, tall oil rosin and mixtures thereof; and polymeric fatty acids derived from bio-renewable resources such as tall oil.

Systems and processes for gas phase-phase synthesis of trisilylamine. One system includes a reactor vessel having a top, bottom, and sidewall having an inner surface. The reactor vessel includes inlets for gaseous reactants, and a gas inlet for an inert gas. In certain reactors the gas inlets are positioned near the top of the reactor vessel and configured to inject the reactant gases in the reactor substantially vertically and downward therefrom. Other reactors are cyclonic-shaped with tangential feeding of the gases. One or more baffles having a peripheral edge and substantially horizontally positioned in the reactor to define a reaction zone above the baffles and a separation zone below the baffles. The baffles are positioned in the reactor vessel such that there is a gap between the baffle peripheral edge and the inner surface of the reactor vessel. Certain systems and processes include mechanical or static mixers.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.−1 to 5 in.sup.−1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.−1)(gal.sup.−1) to 6.0 (lb)(hr.sup.−1)(gal.sup.−1).

A combined reforming apparatus is provided. The combined reforming apparatus includes a body, a plurality of first catalyst tubes disposed inside the body and reacting at a first temperature to reform hydrocarbons (C.sub.xH.sub.y) having two or more carbon atoms into methane (CH.sub.4), a plurality of second catalyst tubes disposed inside the body, connected to the plurality of first catalyst tubes, and reacting at a second temperature higher than the first temperature to reform methane (CH.sub.4) into synthesis gas containing hydrogen (H.sub.2) and carbon monoxide (CO), a combustion unit configured to supply heat to the plurality of first catalyst tubes and the plurality of second catalyst tubes, and a first distributor configured to connect the plurality of first catalyst tubes to each of the second catalyst tubes to distribute steam and gas discharged from the plurality of first catalyst tubes to the plurality of second catalyst tubes.

A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent.

Pressure processing systems disclosed herein comprise rotating fluid flow paths. Transfer of angular momentum between the working fluid and the fluid flow path may be configured to increase pressure within the system and/or recover energy used to increase pressure within the system. Rotation of pressure processing systems may be configured to alter working fluid pressure within the pressure processing system. Filtration and/or chemical processes may be performed within a pressure processing portion of such systems. Working fluid may be introduced or recovered from the system at various radial positions.

Systems, reactors, and processes for regenerating ionic liquid using catalyst. A plurality of tubular reactors are provided having a first end and a second end and catalyst particles disposed in the tubular reactor between the first end and the second end. A line supplies separated ionic liquid catalyst to the first end of the tubular reactor. Hydrogen is also supplied. Regenerated ionic liquid catalyst is recovered from the second end of the tubular reactor. The inner surface of the tubular reactor is preferably non-corrosive or non-reactive. A fluoropolymer lining may be used. The tubular reactors are modular, and may be changed out with the catalyst inside when the catalyst are to be replaced.

Systems, reactors, and processes for regenerating ionic liquid using catalyst. A plurality of tubular reactors are provided having a first end and a second end and catalyst particles disposed in the tubular reactor between the first end and the second end. A line supplies separated ionic liquid catalyst to the first end of the tubular reactor. Hydrogen is also supplied. Regenerated ionic liquid catalyst is recovered from the second end of the tubular reactor. The inner surface of the tubular reactor is preferably non-corrosive or non-reactive. A fluoropolymer lining may be used. The tubular reactors are modular, and may be changed out with the catalyst inside when the catalyst are to be replaced.