The technology relates to a method of producing synthesis gas comprising carbon monoxide (CO) and hydrogen (H.sub.2), wherein the synthesis gas is produced by a reduction reaction of a first flow comprising a carbon source and an excess of hydrogen in contact with an Oxy-flame. The hydrogen comes from a reducing stream, a first portion of which ends up in the first flow, and a second part of which is used to generate the Oxy-flame by combustion of the hydrogen in the presence of a second flow comprising oxygen (O.sub.2), the second flow coming from an oxidizing stream. The first flow and the second flow are at a distance from each other such that the Oxy-flame supports the reaction between the carbon source and the hydrogen. A reactor, which can have different configurations, is also proposed for implementing the method.

An alkylation reaction apparatus has n reactors. In the n reactors, there are m reactors including the first reactor that have three reaction zones as defined below. According to the flow direction order of alkylation reaction streams, the three reaction zones are an x reaction zone, a y reaction zone and a z reaction zone respectively; based on the mixing intensity, the mixing intensity of the y reaction zone>the mixing intensity of the x reaction zone>the mixing intensity of the z reaction zone, wherein n≥1 and n≥m. An alkylation reaction system includes the aforementioned alkylation reaction apparatus, and a liquid acid catalyzed alkylation reaction process by using the aforementioned alkylation reaction apparatus or the aforementioned alkylation reaction system.

Methods and systems for on-site, continuous generation of peracid chemistry, namely peroxycarboxylic acids and peroxycarboxylic acid forming compositions, are disclosed. In particular, an adjustable biocide formulator or generator system is designed for on-site generation of peroxycarboxylic acids and peroxycarboxylic acid forming compositions from sugar esters. Methods of using the in situ generated peroxycarboxylic acids and peroxycarboxylic acid forming compositions are also disclosed.

Combined apparatus (1) for the synthesis of urea from ammonia and carbon dioxide, comprising an internal wall (3) which delimits two coaxial zones (4) inside the apparatus, operating respectively as reaction (4) and condensation (5) zones, and optionally also comprising a stripping zone and/or a scrubber integrated in the same apparatus.

A reactor temperature measurement system includes a Fiber Bragg Grating sensor array arranged in a body of the reactor for monitoring temperatures at multiple positions in an axial direction of the body to obtain temperature sensing optical signals; and a fiber grating demodulator, connected to the Fiber Bragg Grating sensor array, and used to demodulate the temperature sensing optical signals. A method for preparing a Fiber Bragg Grating includes preparing a Fiber Bragg Grating by using a single-mode fiber and annealing the Fiber Bragg Grating, which includes heating the Fiber Bragg Grating to a temperature above 400° C. and maintaining for 100 to 200 hours.

A method for producing a vapor stream from waste plastic comprises providing a waste plastic feedstock into a reactor containing one or more residues produced from a previously heated source of waste plastic, and heating the waste plastic feedstock in the reactor to a temperature from about 125° C. to 500° C. to generate a vapor containing one or more hydrocarbons. The waste plastic feedstock can have a calcium to sodium mass ratio from about 0.0001 to 400 as measured by inductively-coupled plasma (ICP) spectrometry. The catalytic activity in the reactor may be provided through one or more constituent elements in the waste plastic feedstock or the one or more residues produced from the previously heated source of waste plastic.

Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive an anti-solvent, a monomer, and a solvent, and to react the monomer to form a polymer; where the anti-solvent is not a solvent for the polymer and is operative to reduce the lower critical solution temperature; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel and wherein the plurality of devolatilization vessels receives a polymer solution from the reactor system; and a liquid-liquid separator that is operative to receive a polymer solution from the reactor system and to facilitate a separation between the polymer and volatiles by reducing the pressure and temperature of the polymer solution in the liquid-liquid separator.

The present disclosure is generally directed to a new and innovative system, process and method that utilize a new “non-oxygen type of oxidizers” process for methane (CH.sub.4) upgrading to value-added products such as olefins and aromatics (i.e., benzene, toluene and xylene (BTX)) etc. and further removing toxic impurities such as sulphur-containing compounds (i.e. H.sub.2S) by using the sulphur as a source of radical.

The present disclosure relates to a manufacturing system and a manufacturing method which are capable of continuously manufacturing an ester-based composition, and has a technical feature of being capable of manufacturing an ether-based composition continuously, economically, and efficiently.

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).