A process for dehydrating an ethanol feedstock to give ethylene, includes:

a) a vaporization stage;

b) a heating stage;

c) a dehydration stage in a multitubular reactor comprising tubes having a length of between 2 and 4 m, said tubes comprising a, preferably zeolitic, dehydration catalyst, the feedstock having an inlet temperature of greater than 400° C. and less than 550° C. and an inlet pressure of between 0.8 and 1.8 MPa, the heat transfer fluid having an inlet temperature of greater than 430° C. and less than 550° C. and a mass flow rate such that the ratio of the mass flow rates of the heat transfer fluid relative to the feedstock is greater than or equal to 10;

d) separation into an effluent comprising ethylene and an aqueous effluent;

e) purification of the aqueous effluent and separation of a stream of purified water and a stream of unconverted ethanol.

A method of oxidative pyrolysis involves heating hydrocarbon feedstock, heating a steam-oxygen mixture, combusting hydrocarbon feedstock in vapors of a steam-oxygen mixture in a special reactor, rapidly cooling the obtained products of incomplete combustion of chemical reactions in two steps, after which the cooled steam-gas mixture is directed to the fractionation unit. A hydrocarbons pyrolysis device has a steam-oxygen mixture and feedstock mixing chamber, a pyrolysis chamber and a coking reactor, a device for heating hydrocarbon feedstock, a device for heating steam-oxygen mixture coupled to a mixing chamber, a coking reactor having a device for supplying coolant to the pyrogas flow, a separation unit coupled to the coking reactor, a fractionation unit with an additional coolant supply device. Disposal of heavy oil residues by rapid coking with high economic efficiency and environmental safely while obtaining high-quality coke and producing aromatic compounds occurs without construction or additional installations.

A process for dehydrating an ethanol feedstock to give ethylene, includes: a) a vaporization stage; b) a heating stage; c) a dehydration stage in a multitubular reactor comprising tubes having a length of between 2 and 4 m, said tubes comprising a, preferably zeolitic, dehydration catalyst, the feedstock having an inlet temperature of greater than 400° C. and less than 550° C. and an inlet pressure of between 0.8 and 1.8 MPa, the heat transfer fluid having an inlet temperature of greater than 430° C. and less than 550° C. and a mass flow rate such that the ratio of the mass flow rates of the heat transfer fluid relative to the feedstock is greater than or equal to 10; d) separation into an effluent comprising ethylene and an aqueous effluent; e) purification of the aqueous effluent and separation of a stream of purified water and a stream of unconverted ethanol.

Provided herein are absorbent polymers produced from beta-propiolactone, and methods and systems of producing such polymers. The beta-propiolactone may be derived from ethylene oxide and carbon monoxide. The absorbent polymer may be bio-based and/or biodegradable. The absorbent polymers may be used for diapers, adult incontinence products, and feminine hygiene products, as well as for agricultural applications.

A processing system for producing a product material from a liquid mixture includes an array of one or more power jet modules adapted to jet the liquid mixture into one or more streams of droplets and force the one or more streams of droplets into the processing system adapted to process the one or more streams of droplets into the product material. A method for producing a product material from a liquid mixture on a processing system includes moving each of the one or more power jet modules and be connected to an opening of a dispersion chamber, opening one or more doors of the one or more power jet modules, processing the one or more streams of droplets inside a reaction chamber, closing the one or more doors of the power jets modules and moving each of the one or more power jet modules in a second direction.

A method of and apparatus for recovering an alcohol solvent from a liquid mixture of the solvent and plant oil and decarboxylating the plant oil may include, pressurizing the liquid mixture to a super-atmospheric pressure, recirculating the pressurized liquid mixture a plurality of times through at least one membrane separator to separate some of the solvent from the mixture to provide a concentrated mixture of the plant oil with less solvent, reducing the pressure of the liquid concentrated mixture to less than 15 psig, heating it at a pressure of less than 15 psig to a temperature sufficient to vaporize the solvent in the concentrated mixture, removing sufficient heat from the vaporized solvent to condense it to a liquid solvent at atmospheric pressure and temperature conditions, and heating the plant oil to a temperature desirably of at least 215° F. to decarboxylate the plant oil.

The invention relates to Quench box assembly comprising quench pipe and quench box, to mix quench gas and vapor-liquid effluent from previous catalyst bed to achieve equilibrium temperature before entering the next bed. The quench pipe is in the form of ring having aperture while quench box consists of swirling section and a mixing chamber. The swirling section consists of inclined baffles to provide swirling action to incoming stream and the turbulence created by the swirling action increases the heat transfer rate thus requiring the smaller reactor volume to attain equilibrium temperature. The perforated plate being open from all the sides allowing the liquid to flow uniformly from all directions thus providing uniform distribution on the distributor tray. Hence, eliminates the requirement of rough liquid distributor before the distribution tray.

A centric spray pipe apparatus is disclosed, The centric spray pipe includes a plurality of nozzles designed to provide full coverage of liquid spray to a vessel.

A system and a method for producing silicon from a SiO.sub.2-containing material that includes solid SiO.sub.2. The method uses a reaction vessel including a first section and a second section in fluid communication with said first section. The method includes: heating the SiO.sub.2-containing material that includes the solid SiO.sub.2 to a SiO.sub.2-containing material that includes liquid SiO.sub.2, at a sufficient temperature to convert the solid SiO.sub.2 into the liquid SiO.sub.2; converting, in the first section, the liquid SiO.sub.2 into gaseous SiO.sub.2 that flows to the second section by reducing the pressure in the reaction vessel to a subatmospheric pressure; and reducing, in the second section, the gaseous SiO.sub.2 into liquid silicon using a reducing gas. The reducing of the pressure is performed over a continuous range of interim pressure(s) sufficient to evaporate contaminants from the SiO.sub.2-containing material, and removing by vacuum, the one or more evaporated gaseous contaminants.

A system for production of a synthesis gas, including: a synthesis gas generation reactor arranged for producing a first synthesis gas from a hydrocarbon feed stream; a post converter including a catalyst active for catalyzing steam methane reforming, methanation and reverse water gas shift reactions; the post converter including a conduit for supplying a CO.sub.2 rich gas stream into a mixing zone of the post converter, where the CO.sub.2 rich gas stream in the conduit upstream the mixing zone is in heat exchange relationship with gas flowing over the catalyst downstream the mixing zone; a pipe combining the at least part of the first synthesis gas and the CO.sub.2 rich gas stream to a mixed gas, in a mixing zone being upstream the catalyst; wherein the post converter further includes an outlet for outletting a product synthesis gas from the post converter. Also, a corresponding process.