The invention is for use in gas chemistry for producing hydrogen-containing gas on the base of a CO and H.sub.2 mixture (syngas) from natural gas and other hydrocarbon gases. The object of the invention is to suppress side reactions resulting in soot formation when conducting the process in high productivity mode, and also to provide for an uncomplicated reactor design while maintaining compact dimensions thereof. The method for producing a hydrogen-containing gas comprises mixing natural gas with oxygen, partially oxidizing the natural gas with oxygen at a temperature ranging from 1300 C. to 1700 C. resulting in obtaining hydrogen-containing gas, and cooling the stream of the hydrogen-containing gas produced. Said cooling is performed until the temperature drops below 550 C. and at a rate above 100000 C./sec. The reactor comprises the following steps, which are arranged in series along the technological process: means for supplying natural gas and oxygen, a natural gas and oxygen mixing zone, a zone for conducting the reaction by partially oxidizing the natural gas with oxygen, and a zone for cooling the stream of the hydrogen-containing gas produced, which is equipped with a cooling body of revolution in order to provide an intensive cooling of the stream of hydrogen-containing gas by contacting thereof with said body of revolution.

The present disclosure relates generally to processes and systems for dehydrogenating alkanes. The present disclosure relates specifically to processes and systems for dehydrogenating alkanes in which catalyst beds can be cooled rapidly to prevent runaway. In one aspect, a dehydrogenation process includes, when the temperature of at least one of the hybrid catalyst beds becomes higher than a first threshold value during a number of consecutive cycles greater than a second threshold value, reducing the temperature of the oxygen-containing stream by at least 50 C., the reduction of temperature occurring with a temperature drop of at least 50 C. within three minutes.

A method for calcination of a carbon dioxide rich sorbent (containing CaCO.sub.3) includes combusting in a furnace a fuel with an oxidizer, supplying heat transfer (HT) solids into the furnace and heating them, transferring the HT solid particles from the furnace to a reactor having a rotatable container, supplying a carbon dioxide rich solid sorbent (containing CaCO.sub.3) into the rotatable container, rotating the rotatable container for mixing the solid particles and the carbon dioxide rich solid sorbent for transferring heat from the solid particles to the carbon dioxide rich solid sorbent and generating carbon dioxide and carbon dioxide lean solid sorbent (mainly CaO), discharging the carbon dioxide and the carbon dioxide lean solid sorbent from the rotatable container and the subsequent classification of the HT solids from the lean sorbent.

A catalytic converter arrangement for producing phthalic anhydride by means of a gas phase oxidation of aromatic hydrocarbons, comprising a reactor with a gas inlet side for a reactant gas, a gas outlet side for a product gas, a first catalytic converter layer made of catalytic converter elements, and at least one second catalytic converter layer made of catalytic converter elements. The first catalytic converter layer is arranged on the gas inlet side, and the second catalytic converter layer is arranged downstream of the first catalytic converter layer in the gas flow direction. The catalytic converter elements have an outer layer of an active compound. The invention is characterized in that the active compound content in the first catalytic converter layer and/or in the second catalytic converter layer is below 7 wt. %, based on the total weight of the catalytic converter elements, and the ratio of the total surface of the active compound to the volume of the catalytic converter layer is preferably 10000 cm1 to 20000 cm1, in each catalytic converter layer.

The invention relates to a hydrocarbon conversion process and a reactor configured to carry out the hydrocarbon conversion process. The hydrocarbon conversion process is directed to increasing the overall equilibrium production of ethylene from typical pyrolysis reactions. The hydrocarbon conversion process can be carried out by exposing a hydrocarbon feed to a peak pyrolysis gas temperature in a reaction zone in the range of from 850 C. to 1200 C.

In an embodiment, a method of producing a carbonate comprises reacting carbon monoxide and chlorine in a phosgene reactor in the presence of a catalyst to produce a first product comprising phosgene; wherein carbon tetrachloride is present in the first product in an amount of 0 to 10 ppm by volume based on the total volume of phosgene; and reacting a monohydroxy compound with the phosgene to produce the carbonate; wherein the phosgene reactor comprises a tube, a shell, and a space located between the tube and the shell; wherein the tube comprises one or more of a mini-tube section and a second tube section; a first concentric tube concentrically located in the shell; a twisted tube; an internal scaffold; and an external scaffold.

A modular system is configured to generate renewable fuel. The system includes a modular container that has inlets/outlets and houses a treatment subsystem configured to produce treated water and an electrolysis subsystem configured to perform electrolysis of the treated water to produce hydrogen and oxygen. The modular container further includes a reactor configured to perform an exothermic reaction in as little as a single pass using the hydrogen and carbon dioxide to produce the renewable fuel. The modular container can further include a post-processing subsystem configured to perform further processing of the renewable fuel.

A system for using carbonaceous material includes a steam reformer, a hydrocarbon reformer, and at least one gas-cleanup system. Also described are methods of producing liquid fuel and/or chemicals from carbonaceous material.

A heat transfer media comprises a particle. The particle comprises a discontinuous phase and a matrix material. The discontinuous phase is disposed within the matrix material, and the matrix material has a higher melting point than the discontinuous phase. The discontinuous phase has a melting point selected to be within a reaction temperature range.

A fixed bed reactor based on the principle of thermoluminescence to achieve in-situ heat removal and in-situ temperature measurement for strong exothermic reactions can monitor the temperature and heat of the exothermic reaction process from multiple angles, enhance the heat transfer of the catalytic bed layer, and effectively reduce or eliminate the hot spots generated by the exothermic reaction process. This reactor includes a fixed bed reaction tube, and the top of the fixed bed reaction tube is equipped with a xenon lamp pretreatment system, an optical signal detection system, and an infrared temperature measurement system.