Fuel tank inerting systems are described. The systems include a fuel tank having an inerting system flow path connected to the fuel tank. A catalytic reactor is arranged along the inerting system flow path configured to receive a reactant mixture of first reactant and a second reactant to generate inert gas. A condenser heat exchanger is arranged between the catalytic reactor and the fuel tank to cool an output from the catalytic reactor. A first ejector is configured to receive the first reactant and the second reactant and output the reactant mixture through an outlet. A second ejector is configured to receive an inert gas and the second reactant to output a mixture of the second reactant and the inert gas.

A steam methane reformer (SMR) system includes an outer tube, wherein a first end of the outer tube is closed; an inner tube disposed in the outer tube, wherein a first end of the inner tube is open. A flow channel is defined within the inner tube and an annular space is defined between the outer tube and the inner tube, the flow channel being in fluid communication with the annular space. The SMR system includes a catalytic foam disposed in the annular space between the outer tube and the inner tube, the catalytic foam comprising a catalyst.

The application provides in an aspect a process for producing urea in a urea plant comprising a high pressure synthesis section comprising a reactor, wherein the process comprises reacting NH.sub.3 feed and CO.sub.2 feed under urea formation conditions in said reactor to form a urea synthesis solution comprising urea, water, carbamate and ammonia, wherein the process further comprises contacting a carbamate-containing liquid stream with an equipment part of said high pressure synthesis section that is made of a ferritic steel alloy.

Methods for operating a high pressure olefin polymerization reactor include the steps of introducing an initiator stream containing ethylene and an initiator compound through an initiator nozzle into the reactor, introducing an olefin stream containing ethylene and an optional comonomer through an olefin nozzle into the reactor, and polymerizing ethylene and optionally the comonomer in the presence of the initiator stream in the reactor under high pressure polymerization conditions to produce an ethylene polymer. The amount of ethylene in the initiator stream is from 0.01 to 2 wt. % of the amount of ethylene in the olefin stream. An injection nozzle that can be used in conjunction with the high pressure reactor also is described.

Embodiments include a reaction vessel having a reaction chamber defined by opposing first and second interior-facing surfaces of the housing; a first light absorbing layer conforming to the first interior-facing surface of the housing component; and a second light absorbing layer conforming to the second interior-facing surface of the housing component; a first energy source configured to direct light through the housing at the first light absorbing layer; and a second energy source configured to direct light through the housing at the second light absorbing layer.

A built-in micro interfacial enhanced reaction system and process for PTA production with PX are provided. The system includes a reactor and a micro interfacial unit disposed inside reactor. The reactor includes a shell, an inner cylinder concentrically disposed inside shell, and a circulating heat exchange device partially disposed outside shell, inner cylinder having a bottom end connected to inner bottom surface of the shell in closed manner and an open top end, a region between shell and inner cylinder being first reaction zone, inner cylinder containing second reaction zone and third reaction zone from top to bottom, circulating heat exchange device being connected to inner cylinder and micro interfacial unit respectively. The invention can solve problems of large waste of reaction solvent acetic acid under high temperature and high pressure and being unable to take out the product TA in time during existing process of PTA production with PX.

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.

Disclosed herein are processes and reaction systems for controlling a temperature of an oligomerization reaction zone using a heat exchange system.

Heat exchanger-reformer for use in a hydrogen production plant for producing syngas, for instance by means of a steam methane reforming method, wherein the reformer comprises vessel with a first inlet for supplying feed and a second inlet for supplying hot reformer effluent, preferably coming from a main steam methane reformer, wherein the heat exchanger-reformer further comprises a heat exchanging section that is arranged in fluid connection with the first and second inlets for exchanging heat between the feed and reformer effluent to effectuate steam reforming of hydrocarbon to produce syngas, wherein the heat exchanging section comprises a plate heat exchanger assembly for heat exchange between said feed and said reformer effluent.

The process and apparatus of the disclosure utilize a heater between a hydroprocessing reactor and a hydroisomerization reactor. A hydroprocessing feed exchanger cools hydroprocessed effluent to effect turndown of heated hydroprocessed effluent so as to not feed the hydroprocessed effluent to the hydroisomerization reactor at a higher temperature than necessary.