The invention relates to a method for controlling a chemical reaction which creates a product, wherein at least one reactant that is present in a liquid phase is subjected to a pressure change.

Current chemical batch processing technology is based on batch reactors, which typically consist of a vessel, in which reactants are processed. The batch reactor comprises a reactor vessel having at least one first thermal transfer element; a removable top cover for sealing the reactor vessel; a baffle component having at least one second thermal transfer element; and an agitator component, wherein each of the at least one first thermal transfer element and the at least one second thermal transfer element is independently controllable, and wherein the batch reactor comprises a thermal transfer surface-to-volume ratio of at least 6:1. This increases the thermal transfer potential and the thermal energy transfer efficiency of the batch reactor, thereby to increase production speed and throughput.

The machinery and methods disclosed herein are based on the use of a specialized extruder configured to continuously convey and plasticize/moltenize selected lignocellulosic biomass and/or waste plastic materials into a novel variable volume tubular reactor, wherein the plasticized/moltenized material undergoes reaction with circumferentially injected supercritical water—thereby yielding valuable simple sugar solutions and/or liquid hydrocarbon mixtures (e.g., “neodiesel”), both of which are key chemical commodity products. The reaction time may be adjusted by changing the reactor volume. The machinery includes four zones: (1) a feedstock conveyance and plasticization/moltenization zone; (2) a steam generation and manifold distribution zone; (3) a central supercritical water reaction zone; and (4) a pressure let-down and reaction product separation zone. The machinery and methods minimize water usage—thereby enabling the economic utilization of abundant biomass and waste plastics as viable renewable feedstocks for subsequent conversion into alternative liquid transportation fuels and valuable green-chemical products.

Chemical reactors (10) and methods crack hydrocarbons in process fluids by accelerating the process fluid to a velocity greater than Mach 1 with an axial impulse impeller (40) and generating a shock wave (90) in the process fluid by decelerating it in a static diffuser (70) having diverging diffuser passages (72). Temperature increase of the process fluid downstream of the shockwave cracks the entrained hydrocarbons in a single pass, through a unidirectional flow path (F), within a single stage, without recirculating the process fluid for another pass through the same stage. In some embodiments, the turbomachine chemical reactor (110) has multiple successive stages of one or more axial impulse impellers (40A, 40B), paired with a diverging passage, static diffuser (70). Successive stages crack additional hydrocarbons by successively raising temperature of the flowing process fluid.

Chemical reactor with high speed rotary mixing, system thereof, and method thereof, for catalytic thermal conversion of organic (hydrocarbon-containing) materials (coal, plastics, rubber, plant matter, wood shavings, biomass, organic wastes) into diesel and other liquid fuels (automobile or/and jet engine fuels). Relevant to non-conventional commercial scale production of liquid fuels, and to commercial scale processing and disposing of organic waste materials. Chemical reactor includes: integrated combination of a reactor stationary assembly (RSA), having only stationary components remaining stationary during chemical reactor operation, and a reactor rotary mixing assembly (RRMA), having only rotatable components rotating during chemical reactor operation. May include anti-abrasion shield for shielding inner surface of reactor central housing from abrasion during chemical reactor operation. Rotor may include a reinforcement disc. Rotor blades or/and reinforcement disc may include rotor-based performance and process control structural features (openings, or/and protrusions, or/and depressions), for additionally controlling performance of the rotor.

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.

Process for the preparation of styrenic polymers having an improved color stability by anionic polymerization wherein the obtained terminated polymer solution is fed to a dispersing device to which water is added, fed to a buffer vessel and then is impregnated in a static mixer by addition of further water, carbon dioxide and one or more stabilizers.

Chemical reactors (10) and methods crack hydrocarbons in process fluids by accelerating the process fluid to a velocity greater than Mach 1 with an axial impulse impeller (40) and generating a shock wave (90) in the process fluid by decelerating it in a static diffuser (70) having diverging diffuser passages (72). Temperature increase of the process fluid downstream of the shockwave cracks the entrained hydrocarbons in a single pass, through a unidirectional flow path (F), within a single stage, without recirculating the process fluid for another pass through the same stage. In some embodiments, the turbomachine chemical reactor (110) has multiple successive stages of one or more axial impulse impellers (40A, 40B), paired with a diverging passage, static diffuser (70). Successive stages crack additional hydrocarbons by successively raising temperature of the flowing process fluid.

Provided is a method for manufacturing a polymer by a flow-type reaction, including introducing a liquid A containing an anionic polymerizable monomer and a non-polar solvent, a liquid B containing an anionic polymerization initiator and a non-polar solvent, a liquid C containing a polar solvent, and a polymerization terminator into different flow paths; allowing the liquids to flow in the respective flow paths; allowing the liquid A and the liquid B to join together at a joining portion; allowing a conjoined liquid M.sup.AB of the liquid A and the liquid B to join with the liquid C at downstream of the joining portion; subjecting the anionic polymerizable monomer to anionic polymerization while a conjoined liquid M.sup.ABC of the conjoined liquid M.sup.AB and the liquid C is flowing to downstream in a reaction flow path; and allowing a polymerization reaction solution flowing in the reaction flow path to join with the polymerization terminator so that the polymerization reaction is terminated and a polymer is obtained, in which a polarity of a solvent of the liquid M.sup.ABC is made higher than a polarity of a solvent of the liquid M.sup.AB. Also provided is a flow-type reaction system suited for performing the manufacturing method.

A continuous tubular reactor includes a rotary reaction tube having a reactant inlet and a product outlet, and including a ceramic; a heating device disposed outside the rotary reaction tube; and an angle adjuster adjusting an angle of a rotation axis of the rotary reaction tube. The angle of the rotation axis is 75 or less with respect to a horizontal surface.