A continuous chemical reactor may include a primary reaction unit and at least one secondary reaction unit. The primary reaction unit has a stirring device and a first temperature regulating device, and a feed inlet provided at an upper portion thereof. The secondary reaction unit is sleeved outside the primary reaction unit, and a reaction chamber is formed therebetween. By adding reaction materials to the primary reaction unit via the feed inlet and adjusting the temperature of the reaction materials by the first temperature regulating device, the reacted materials enter the reaction chamber, and the heat generated in the reaction chamber can be used to adjust the temperature of the materials in the primary reaction unit to more effectively use the heat, and the product after reaction can be discharged from a discharge hole at the lower end of the secondary reaction unit, thereby achieving continuous production.

An apparatus for the destruction of a precursor material includes a steam plasma reactor having a high temperature zone and a combustion zone. The high temperature zone is adapted for hydrolyzing the precursor material, whereas the combustion zone is adapted to effect medium temperature oxidation of the reactant stream where combustion oxygen or air is injected. A quenching unit is provided at an exit end of the reactor for quenching a resulting gas stream to avoid the formation of unwanted by-products.

Disclosed is a solution polymerization process, or, alternatively, a method of delivering powder catalysts to a solution polymerization reactor, comprising combining a homogeneous single-site catalyst precursor with -olefin monomers to form a polyolefin, wherein the homogeneous single-site catalyst precursor is in the form of (i) a dry powder, (ii) suspended in a aliphatic hydrocarbon solvent, or (iii) suspended in an oil or wax, wherein the homogeneous single-site catalyst precursor is at a concentration greater than 0.8 mmole/liter when suspended in the aliphatic hydrocarbon solvent prior to entering the solution polymerization reactor.

Disclosed is a solution polymerization process, or, alternatively, a method of delivering powder catalysts to a solution polymerization reactor, comprising combining a homogeneous single-site catalyst precursor with -olefin monomers to form a polyolefin, wherein the homogeneous single-site catalyst precursor is in the form of (i) a dry powder, (ii) suspended in a aliphatic hydrocarbon solvent, or (iii) suspended in an oil or wax, wherein the homogeneous single-site catalyst precursor is at a concentration greater than 0.8 mmole/liter when suspended in the aliphatic hydrocarbon solvent prior to entering the solution polymerization reactor.

A raw material fluid treatment plant provided with a raw material reaction apparatus for reacting a raw material fluid to form a reaction gas. The raw material reaction apparatus includes preheaters and a reactor. The preheaters are heat exchangers that perform heat exchange between a second heat transfer medium and the raw material fluid to heat the raw material fluid. The reactor is a heat exchanger that performs heat exchange between a first heat transfer medium differing from the second heat transfer medium and the raw material fluid having been heated by the preheaters to heat and react the raw material fluid.

The present disclosure relates to processes, methods, systems, and apparatus for steam cracking hydrocarbon in a pyrolysis furnace having a convection zone and a radiant zone. The convection zone includes three heat exchangers in series with a serpentine arrangement. A fluid source is disposed each heat exchanger to provide steam into the heat exchangers. The present disclosure further relates to a process of adjusting the stream flow rate for each fluid source to control operating conditions such as flue gas temperature, stack temperatures, and temperatures of other components of the furnace.

The invention relates to a reactor for performing exothermic equilibrium reactions, especially for producing methanol from synthesis gas in a multistage synthesis with intermediate condensation of the reaction product. The reactor according to the invention has a reactor shell and a multitude of series-connected and mutually fluid-connected reactor cells disposed within the reactor shell, where each of the reactor cells includes a reaction apparatus, a cooling-down apparatus and a phase separation apparatus as reactor cell elements. The reactor has a multitude of reactor planes disposed in a mutually parallel arrangement within the reactor shell, where reactor cell elements of the same kind are disposed in the same reactor plane. The inventive arrangement of the reactor cell elements enables the building of a compact reactor and reduces material stresses within the reactor by the avoidance of large temperature differences within the reactor shell.

A process and apparatus for the continuous conversion of isotropic carbonaceous materials into anisotropic mesophase pitch is disclosed. The invention disclosed herein addresses the need for lower production costs compared with traditional batch mesophase conversion of isotropic pitch. A unique thermal processing and in-process separation of reacted mesophase from the continuous matrix of fresh or partially reacted isotropic pitch is provided. Potential uses are for further continuous processing into carbon fibers or carbon form densification.

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 n1 and nm. 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.

A water gas shift (WGS) reactor system includes a housing; a reaction tube disposed in the housing, wherein a reaction channel is defined within the reaction tube and a cooling fluid channel is defined between the housing and the reaction tube; a catalyst disposed in the reaction channel, the catalyst configured to catalyze a hydrogen generation reaction; and a heat transfer material disposed in the reaction channel.