A forced thin film-type flow reactor that, in addition to a pressure balancing mechanism with which it is possible to set and adjust the clearance between processing surfaces using pressure balancing, is provided with a clearance adjustment mechanism that allows the clearance to be set and adjusted by an alternative means. The flow reactor processes a fluid to be processed by passing the fluid to be processed between a first processing surface and a second processing surface disposed so as to be capable of moving towards and away from each other, and the flow reactor comprises a pressure balancing mechanism and a mechanical clearance mechanism. The pressure balancing mechanism forms a minute first clearance by providing pressure balance between the pressure applied by the fluid to be processed, which acts in the direction in which the first processing surface and the second processing surface move away from each other, and a force produced by a back pressure mechanism, which acts in the direction in which the first processing surface and the second processing surface move towards each other. The mechanical clearance mechanism mechanically sets a second clearance, which is greater than the first clearance, and makes it possible to set the clearance irrespective of the pressure of the fluid to be processed.

In accordance with one embodiment, a processing device includes a heated internal wall and a rotating rod positioned within an interior space formed by the heated internal wall. The rotating rod may be hollow and act as an internal heat exchanger. The processing device also includes a plurality of baffles spaced apart from one another along the rotating rod and extending away from the rotating rod towards the heated internal wall. The plurality of baffles or porous, packed basket that rotates with the rotating rod that also may be configured to provide cooling relative to the heated internal wall. The processing device also includes at least one wiper or roller coupled to an edge of at least one of the plurality of baffles or porous, packed basket, coupled to the rotating rod and that contacts the heated internal wall while rotating together with the rotating rod. In another embodiment, a processing device may be used to adsorb reactive gases into a liquid phase while heat is exchanged.

A method and apparatus are provided for processing hydrocarbon coal slurry feeds. The method and apparatus enhance the conversion of the coal feeds into useful conversion products, such as high melting and high carbon containing pitch products. In particular, the present techniques utilize a specially designed “self-cleaning” and “wall-catalyzed” preheater-reactor systems.

The present invention relates generally to the generation of bio-products from organic matter feedstocks. More specifically, the present invention relates to improved methods for the hydrothermal/thermochemical conversion of lignocellulosic and/or fossilised organic feedstocks into biofuels (e.g. bio-oils) and/or chemical products (e.g. platform chemicals).

A device for the descending flow of a hydrocarbon-containing liquid containing solid particles at the bottom of an item of equipment (1) and a process for the conversion of hydrocarbon-containing feedstocks implementing said device.

A process and system for cleaning a high pressure separator vessel in a polymerization reactor without removing the top cover and its associated bolts by providing a cleaning hole in a fluid fitting above and adjacent to the top cover, through which a cord or cable is fed and affixed to a rotatable cleaning nozzle. The cleaning nozzle is gradually raised, lowered and rotated to direct a high pressure liquid onto the interior walls of the vessel to remove accumulated waste material.

There are provided methods of treating a catalyst-containing reactor system with a liquid solvent to remove contaminants from the reactor system. An exemplary method includes the steps of: isolating the reactor system to be treated from upstream and downstream equipment; reducing the temperature and pressure of the isolated reactor system by flushing with a hydrogen rich gas; injecting a non-aqueous liquid solvent into the reactor system at an injection point while continuously flowing hydrogen-rich gas through the reactor system; maintaining the solvent in a liquid state while flowing the solvent continuously through the reactor system; and terminating the step of injecting solvent and terminating the continuous flowing of hydrogen-rich gas. The exemplary method is free of the injecting of a carrier gas into the reactor system comprising alkanes selected from the methane, ethane, propane, butane and pentane.

A direct decomposition device for hydrocarbons for directly decomposing hydrocarbons into carbon and hydrogen includes a rector containing a catalyst including a plurality of metal particles with an iron purity of 86% or more. The reactor is configured to be supplied with a raw material gas containing hydrocarbons.

A system and method for a first reactor to produce a transfer slurry having a first polyolefin polymerized in the first reactor, a heat-removal zone to remove heat from the transfer slurry, and a second reactor to receive the transfer slurry cooled by the heat-removal zone, the second reactor to produce a product slurry having a product polyolefin which includes the first polyolefin and a second polyolefin polymerized in the second reactor.

Methods and systems for using temperature measurements taken from a compact insulated skin thermowell to optimize a pyrolysis reaction are provided. In the present systems and methods, the upstream temperature and the upstream pressure of a pyrolysis reactor is measured through an adiabatic restriction in the inlet manifold of a parallel tube assembly to provide an absolute upstream temperature and an upstream pressure. The downstream temperature of the pyrolysis reactor is also measured following an adiabatic restriction to provide an absolute downstream temperature. The downstream pressure is then determined by multiplying the absolute upstream pressure with the quotient of the downstream temperature divided by the upstream temperature as taken to the power of k/k1, where k is the ratio of fluid specific heat at constant pressure (Cp) to fluid specific heat at constant volume (Cv).