Processes and systems for making cyclopentadiene and/or dicyclopentadiene include converting acyclic C5 hydrocarbon(s) into CPD in a first reactor to obtain a first reactor hydrocarbon effluent, which is processed in an eductor to obtain an eductor effluent at higher total pressure than atmospheric pressure, separating the eductor effluent in a separator such as compression train to obtain a C5-rich fraction comprising CPD, dimerizing the C5-rich fraction in a second reactor to obtain a product effluent comprising DCPD, which is separated to obtain a DCPD-rich fraction. Multiple-stage of dimerization and separation steps can be optionally used to obtain multiple DCPD-rich fractions of various degrees of purity and quantity. C5-rich fractions from various stages of the process may be recycled to the first reactor, or converted into mogas components after selective hydrogenation. C5-rich fractions and mogas components may be optionally separated to produce value-adding chemicals.

Processes and systems for making cyclopentadiene and/or dicyclopentadiene include converting acyclic C5 hydrocarbon(s) into CPD in a first reactor in the presence of a C1-C4 co-feedstock to obtain a product mixture, separating the product mixture in a separation sub-system such as compression train to obtain a C5-rich fraction comprising CPD and essentially depleted of hydrogen and C1-C4 hydrocarbons, dimerizing the C5-rich fraction in a dimerization reactor to obtain a product effluent comprising DCPD, followed by separating the product effluent to obtain a DCPD-rich fraction. Multiple-stage of dimerization and separation steps can be optionally used to obtain multiple DCPD-rich fractions of various degrees of purity and quantity. C5-rich fractions from various stages of the process may be recycled to the first reactor, or converted into mogas components after selective hydrogenation. C5-rich fractions and mogas components may be optionally separated to produce value-adding chemicals.

The invention relates to converting non-aromatic hydrocarbon in the presence of CO.sub.2 to produce aromatic hydrocarbon. CO.sub.2 methanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading.

The principles and embodiments of the present invention relate to methods and systems for safely providing NO to a recipient for inhalation therapy. There are many potential safety issues that may arise from using a reactor cartridge that converts NO.sub.2 to NO, including exhaustion of consumable reactants of the cartridge reactor. Accordingly, various embodiments of the present invention provide systems and methods of determining the remaining useful life of a NO.sub.2-to-NO reactor cartridge and/or a breakthrough of NO.sub.2, and providing an indication of the remaining useful life and/or breakthrough.

A multistage tubular reaction system and method for preparing methylol derivatives of an aldehyde includes a tubular reaction system with a plurality of successive reactor stages comprising a plurality of jacketed reaction tubes provided with a cooling system adapted to control flow of a cooling medium through said jacketed reaction tubes. The cooling medium flow is controlled independently in different stages in response to temperature measurements in the reaction system to regulate temperature. In order to further reduce temperature spikes and byproduct generation, aldehyde is stepwise added to the production stream at a plurality of feed ports proximate to reaction tubes equipped with tube inserts to enhance mixing and heat transfer.

A method for revamping a secondary reformer (1), the reformer comprising an internal gas riser pipe (8) for routing a process gas from a bottom gas inlet to a combustion chamber (5) located above a catalytic zone (6), and a distributor (9) for introduction of an oxidation agent such as process air into the combustion chamber. The original distributor of the oxidation agent is discontinued, the gas riser pipe is shortened (8) and the outlet end of the shortened gas riser pipe is arranged to deliver a gas flow directed upwards. A new burner (20) is installed on top of the reformer, the new burner being arranged to deliver an oxidation agent such as process air with a downward flow, thus obtaining a counterflow mixing zone (23) and formation of a diffusion flame above the outlet end of the gas riser pipe.

The present disclosure relates in a broad form to a pseudo-isothermal flow reactor (100) for an exothermal reaction comprising at least two reaction enclosures (108, 114) and a cooling medium enclosure (102) configured to hold a cooling medium under pressure at the boiling point of said cooling medium, said reaction enclosures (108, 114) having an outer surface configured to be in thermal contact with the cooling medium, and each of said reaction enclosures (108, 114) having an inlet and an outlet with the associated benefit of enabling a two-stage pseudo-isothermal operation while only requiring a single cooling medium enclosure (102) and only single cooling medium circuit.

A method for generating and for fusing ultra-dense hydrogen in which molecular hydrogen is fed into at least one cavity and catalyzed, where the splitting and subsequent condensation of the molecular hydrogen is initiated on a catalyst of the cavity to form an ultra-dense hydrogen. The ultra-dense hydrogen is exposed to pressure or electromagnetic radiation to initiate fusion of the ultra-dense hydrogen in the at least one cavity and the reaction heat is led out from the at least one cavity. The pressure as mechanical resonance or the electromagnetic radiation as electromagnetic resonance amplifies the field and therefore the effect. Also, an apparatus for carrying out the method is disclosed.

A material arrangement for a fusion reactor comprising at least one material which is configured as a foam-like carrier material for condensable binding and fusing of hydrogen. The carrier material is provided with positively charged vacancies for condensing hydrogen atoms, small pores for receiving the condensate and for accelerating the condensation after previous penetration of atoms or molecules into these, and large pores for transporting a catalyst into the small pores. Furthermore, a method for producing the material arrangement is disclosed.

A process for reducing the environmental contaminants in a ISO 8217:2017 Table 2 compliant Feedstock Heavy Marine Fuel Oil and resulting product, the process involving: mixing a Feedstock Heavy Marine Fuel Oil with a Activating Gas to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture; separating the Product Heavy Marine Fuel Oil from the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil complies with ISO 8217:2017 Table 2 for residual marine fuel and the Environmental Contaminants, which are selected from the group consisting of: a sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, are less than 0.5 wt. %. The Product Heavy Marine Fuel Oil can be used as blending stock for an ISO 8217:2017 Table 2 compliant, IMO 2020 compliant, low sulfur heavy marine fuel composition.