The present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps: i) providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.

An anti-coking surface having a thickness up to 15 microns comprising from 15 to 50 wt. % of MnCr.sub.2O.sub.4 (for example manganochromite); from 15 to 25 wt. % of Cr.sub.0.23Mn.sub.0.08Ni.sub.0.69 (for example chromium manganese nickel); from 10 to 30 wt. % of Cr.sub.1.3Fe.sub.0.7O.sub.3 (for example chromium iron oxide); from 12 to 20 wt. % of Cr.sub.2O.sub.3 (for example eskolaite); from 4 to 20 wt. % of CuFe.sub.5O.sub.8 (for example copper iron oxide); and less than 5 wt. % of one or more compounds chosen from FeO(OH), CrO(OH), CrMn, Si and SiO.sub.2 (either as silicon oxide or quartz) and less than 0.5 wt. % of aluminum in any form provided that the sum of the components is 100 wt. % is provided on steel.

An anti-coking surface having a thickness up to 15 microns comprising from 15 to 50 wt. % of MnCr.sub.2O.sub.4 (for example manganochromite); from 15 to 25 wt. % of Cr.sub.0.23Mn.sub.0.08Ni.sub.0.69 (for example chromium manganese nickel); from 10 to 30 wt. % of Cr.sub.1.3Fe.sub.0.7O.sub.3 (for example chromium iron oxide); from 12 to 20 wt. % of Cr.sub.2O.sub.3 (for example eskolaite); from 4 to 20 wt. % of CuFe.sub.5O.sub.8 (for example copper iron oxide); and less than 5 wt. % of one or more compounds chosen from FeO(OH), CrO(OH), CrMn, Si and SiO.sub.2 (either as silicon oxide or quartz) and less than 0.5 wt. % of aluminum in any form provided that the sum of the components is 100 wt. % is provided on steel.

In various embodiments, a microreactor features a corrosion-resistant microchannel network encased within a thermally conductive matrix material that may define therewithin one or more hollow heat-exchange conduits.

Methods and apparatus are disclosed for triggering an exothermic reaction under a high hydrogen loading rate. It is generally understood that a high hydrogen loading ratio is an important factor. The present application teaches that a high hydrogen loading rate, that is, achieving a high hydrogen loading ratio in a short period of time, is another important factor in determining whether excess heat can be observed in an exothermic reaction. The present application discloses methods and apparatus for achieving a high hydrogen loading rate in order to trigger an exothermic reaction.

A reactor shell for producing olefins via steam cracking from a fed reactive mixture stream composed of steam and hydrocarbons comprising: at least one reactive stream duct formed within said reactor shell, at least one structured ceramic bed having a plurality of hollow flow paths, at least one electrical resistance heating element for heating the reactive mixture stream up to a predetermined reaction temperature and a coating provided on a surface contacting with the reactive mixture stream is provided. The reactor shell is characterized by that said electrical resistance heating element that is arranged inside at least some of said hollow flow paths in a manner that there still remains a flowing passage inside the hollow flow paths.

The present invention relates to a process for modifying the fluorine distribution in a hydrocarbon compound, comprising a step of making contact between said hydrocarbon compound and a catalytic composition comprising a chromium-based catalyst, said process being performed in a reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being laid against each other by bonding.

The invention relates to a process for the positioning of a corrosion-resistant coating on an internal or external metal wall (20) of a fluid catalytic cracking unit chamber, comprising: (i) the shaping of a metal anchoring structure (10) formed from a plurality of strips (12) assembled in pairs by joining assembly portions (121, 122) so as to form a plurality of cells (14), the anchoring structure comprising a plurality of fastening tabs (16) integral with strip portions other than assembly portions, (ii) the fastening of said anchoring structure (10) by welding the free edge (18) of a part at least of the fastening tabs to the metal wall (20), defining a space between a longitudinal edge (12b) of an anchoring structure and the metal wall, (iii) the insertion of a composite material into the cells (14) from the metal wall (20) and at least up to the upper longitudinal edge (12a) of each strip.

In various embodiments, a microreactor features a corrosion-resistant microchannel network encased within a thermally conductive matrix material that may define therewithin one or more hollow heat-exchange conduits.

The present invention relates to a process for producing 2-chloro-3,3,3-trifluoropropene, comprising the steps: i) providing a stream A comprising at least one chlorinated compound selected from the group consisting of 2,3-dichloro-1,1,1-trifluoropropane, 1,1,1,2,3-pentachloropropane, 1,1,2,3-tetrachloropropene and 2,3,3,3-tetrachloropropene; and ii) in an adiabatic reactor comprising a fixed bed composed of an inlet and an outlet, bringing said stream A into contact, in the presence or absence of a catalyst, with HF in order to produce a stream B comprising 2-chloro-3,3,3-trifluoropropene, characterized in that the temperature at the inlet of the fixed bed of said adiabatic reactor is between 300° C. and 400° C. and the longitudinal temperature difference between the inlet of the fixed bed and the outlet of the fixed bed of said reactor is less than 20° C.