Abstract: Device for connecting a heat exchange pipe (4), whereby said pipe (4) is positioned between walls (11) that are located on both sides of pipe (4), intended for heating and/or cooling a reactor, whose internal pressure is considerably higher than the atmospheric pressure and than the pressure that prevails inside said pipe (4), and said reactor, whereby said device comprises a series of cooperating means that comprise: means for connecting this pipe (4) and jacket (2a) of said reactor, whereby said means comprise a packing box (21, 22, 23), a flange (28) that is attached to jacket (2a) of the reactor by means of a joint (18), a bellows (25) that is placed between packing box (21, 22, 23) and said flange (28) to ensure a relatively flexible connection between pipe (4) and jacket (2a) of the reactor. FIG. 3 to be published.

Abstract: A steam-cracking process with a very high degree of severity of a feedstock that comprises at least 20% by weight of hydrocarbons of the group that is formed by ethane and propane in which the feedstock that is diluted with water vapor is circulated in the radiation zone of a furnace, in at least one pipe with a length L≧14 m and a hydraulic diameter that is greater than or equal to 34 mm in the end portion of the pipe at least, is described under the following conditions of dwell time &tgr; and furnace output temperature COT: 120 ms≦&tgr;≦2800 ms and 858° C.≦COT≦1025° C. to obtain a conversion of at least 77% of ethane of the feedstock if the feedstock contains ethane and/or a conversion of at least 96% of the propane of the feedstock if the feedstock contains propane, and to maintain this conversion for a cycle time that is greater than or equal to about 8 days.

Abstract: A process for producing methylacetylene and propadiene in a reaction zone which is elongate in one direction (one axis) comprises a heating zone and a cooling zone following said heating zone, in which a gas mixture comprising at least one hydrocarbon containing at least three carbon atoms e.g. propane and/or propylene from stream cracking, and at least one diluent is circulated in the heating zone, under super-atmospheric pressure, in a flow direction substantially parallel to the direction (to the axis) of the heating zone, wherein the heating zone comprises at least one preheating zone in which the temperature of said gas mixture increases by about 50° C. to 120° C. per {fraction (1/10)} of the length of the heating zone, at least one pyrolysis zone for the feed in which the temperature rises by about 20° C. to 50° C. per {fraction (1/10)} of the length of the heating zone and at least one methylacetylene-propadiene formation zone in which the temperature climbs by about 70° C.

Abstract: A continuous pyrolysis and decoking process and apparatus is described for the production of acetylenic compounds, in which hydrocarbons and steam are circulated in at least one tube (31) of a steam cracking reactor (30) and steam is circulated in at least one tube (32) of that reactor. The hydrocarbon effluent and steam then circulate in at least one row (1) of a pyrolysis reactor (40) and the decoking effluent comprising steam circulate in at least one other row (2) of that reactor (4) to effect decoking. A set of valves V1, V2, V11, V12 is used to alternate the pyrolysis step path and the decoking step path. The temperature in the steam cracking furnaces is lower than that in the pyrolysis reactor.

Abstract: Device for connecting a heat exchange pipe (4), whereby said pipe (4) is positioned between walls (11) that are located on both sides of pipe (4), intended for heating and/or cooling a reactor, whose internal pressure is considerably higher than the atmospheric pressure and than the pressure that prevails inside said pipe (4), and said reactor, whereby said device comprises a series of cooperating means that comprise: means for connecting this pipe (4) and jacket (2a) of said reactor, whereby said means comprise a packing box (21, 22, 23), a flange (28) that is attached to jacket (2a) of the reactor by means of a joint (18), a bellows (25) that is placed between packing box (21, 22, 23) and said flange (28) to ensure a relatively flexible connection between pipe (4) and jacket (2a) of the reactor.

Abstract: A process for thermal pyrolysis of a feedstock containing at least 80% ethane to convert to ethylene at a conversion rate of at least equal 80% by feeding the feedstock into a reaction zone in which heating means are arranged approximately perpendicular to the direction of flow of the feedstock. The temperature of the outlet of the heating zone in the reaction zone is between 880 and 960° C. and the dwell time of the feedstock in the heating zone is between 1005 and 3000 milliseconds.

Abstract: Described in a process for hydrotreating (HDT) a petroleum feedstock (1) that contains sulfur and nitrogen are the catalytic cracking of the ammonia, produced by the hydrotreating process, in a catalytic cracking furnace (F), the cooling (E2) and separating of the cracking effluent to produce an H.sub.2 S containing gas phase, the extraction of the hydrogen sulfide from said gas phase and from the hydrotreating purge gas in an amine washing unit (20), and the separation (SM) of the hydrogen from the resultant effluent. The recovered hydrogen is recycled to hydrotreating unit (HDT) via a pipe (17).

Abstract: A process for the pyrolysis of hydrocarbons in a reactor with at least two rows which are parallel to each other in which at least one row is supplied with a non hydrocarbon fluid containing steam to decoke the reaction zone at least in part. At least one other row is supplied with a gaseous mixture containing at least one hydrocarbon and water, to pyrolyze said mixture.

Abstract: A continuous pyrolysis and decoking process and apparatus is described for the production of acetylenic compounds, in which hydrocarbons and steam are circulated in at least one tube (31) of a steam cracking reactor (30) and steam is circulated in at least one tube (32) of that reactor. The hydrocarbon effluent and steam then circulate in at least one row (1) of a pyrolysis reactor (40) and the decoking effluent comprising steam circulate in at least one other row (2) of that reactor (4) to effect decoking. A set of valves V1, V2, V11, V12 is used to alternate the pyrolysis step path and the decoking step path. The temperature in the steam cracking furnaces is lower than that in the pyrolysis reactor.

Abstract: A process is described for the catalytic cracking of ammonia present in a fluid containing hydrogen sulphide, in which the fluid is introduced into a reactor comprising a suitable catalyst and a catalytic cracking effluent is recovered. The temperature in the reaction zone is 1000.degree. C. to 1400.degree. C. and a reactor for carrying out the process comprises at least one heating chamber (3, 4) and at least one catalysis chamber (11) in which the ammonia is cracked without cracking the hydrogen sulphide. In a further variation, the reactor comprises at least one catalyst in the spaces defined between the heating elements.

Abstract: A process for the extraction of hydrogen sulphide from a gas mixture comprises: a step (a) in which the gas mixture is passed into an aqueous acidic solution of copper sulphate under conditions which lead to the formation of copper sulphide; a gas which is highly depleted in hydrogen sulphide and an aqueous phase containing copper sulphide in suspension are recovered; a step (b) in which the copper sulphide contained in suspension in the aqueous phase from step (a) is oxidised using an oxygen-containing gas under conditions which lead to the formation of solid elemental sulphur and soluble copper sulphate from this liquid phase; and a step (c) in which the solid sulphur and the solid copper sulphide which is not transformed during step (b) are separated and at least a portion of the aqueous acidic phase containing the copper sulphate formed during step (b) is optionally recycled to step (a).The process is used to absorb hydrogen sulphide contained in a variety of industrial gases.

Abstract: The invention relates to an apparatus comprising a reactor, elongated along one axis, preferably of square or rectangular cross section. The reactor has, at one extremity, at least one supply line for at least one reactant and at least one evacuation outlet at the other extremity for removal of produced effluents. In a first zone (near the first extremity of the reactor), a plurality of heat exchangers, substantially parallel to each other, are disposed in substantially parallel layers perpendicular to the reactor axis, thereby defining spaces or passages for circulation of reactant(s) and/or effluents between the heat exchangers and/or layers formed by the heat exchanger. The heat exchangers are adapted to exchange heat in the passages through successive transverse sections, which are independent and substantially perpendicular to the reactor axis.

Abstract: A process for the thermal pyrolysis of hydrocarbons in a reactor (1) of elongate shape comprising at a first end supply means (5) for a gaseous mixture containing at least one hydrocarbon, at the opposite end discharge means (10) for the effluents produced and between these two ends supply means (9) for effluent cooling fluid, the reactor comprising in a first part (first end side) a plurality of electric heating means (3) enclosed by casings (4) disposed in substantially mutually parallel layers perpendicular to the axis of the reactor, in such a way as to define between the casings and/or the casings and the walls (22), spaces or passages for circulation of the gaseous mixtures and/or effluents. The heating means heat the passages in successive, individual, transverse sections which are substantially perpendicular to the axis of the reactor. The reactor comprises means for introducing into the casings (4) a gas G known as a casing gas which preferably contains water vapour and/or hydrogen.

Abstract: Apparatus suitable for the thermal conversion of methane to hydrocarbons of higher molecular weight, comprising an elongated reactor 1 provided with an inlet 5 for supplying a gas mixture containing methane (process gas) and an outlet at the opposite end, the reactor over a first part towards the inlet end having a plurality of electric heaters 3 surrounded by sheaths 4. The heaters, e.g., electric resistors, which are spaced apart and are substantially parallel with respect to one another, are arranged in substantially parallel rows perpendicular to the axis of the reactor so as to permit circulation of the process gas and/or effluent between the sheaths and/or between the sheaths and walls 22 separating two consecutive rows. The heaters heat the passages by successive independent cross sections substantially perpendicular to the axis of the reaction. Towards the outlet end, the reactor further comprises an injector for supplying cooling fluid, which cools the effluent.

Abstract: A process and reactor are disclosed for the thermal cracking of a charge containing at least one hydrocarbon with at least one carbon atom, in which the charge is circulated in a metal reaction zone which includes a pyrolysis zone whose external wall is in thermal exchange relationship with a heating liquid. The reaction zone consists of an alloy containing, by weight, 66-82% nickel, 14-18% chromium, and 4-6% aluminum. This alloy, which has already been preoxidized, may be covered, at least in the reaction zone, with at least one layer formed by an oxide of at least one metal and/or at least one metal carbide and/or at least one metal nitride and/or at least one metal silicide. The invention finds application for vapor-phase cracking and dehydrogenation of hydrocarbon charges.

Abstract: For preparing at least one boric oxide in an anhydrous or hydrated form and of general formula B.sub.2 O.sub.3, xH.sub.2 O, in which x is a number from 0 to 3, a methyl borate hydrolyzate comprising boric oxide and methanol is introduced into a distillation column is introduced the product from, at least one compound (preferably a hydrocarbon such as, e.g., 2,3-dimethyl butane or 2-methyl pentane) forming a heteroazeotrope with methanol, said heteroazaeotrope having a boiling point below that of the azeotrope formed by methyl borate with methanol and at least one compound having a boiling point higher than that of methyl borate, said compound not forming an azeotrope with a boiling point below that of said heteroazeotrope and then at the head of the column said heteroazeotrope is recovered and at the bottom of the column a suspension containing at least one boric oxide.

Abstract: An oxidation reactor having elongated shape includes in combination, a mixing member including a pipe for feeding oxidizing gas and a pipe for feeding oxidizable charge; a reaction member, arranged subjacent the mixing member, and a discharge member associated with a discharge pipe for the products of the reaction. The reaction member includes a central zone which has a first lining and the reactor includes at least one peripheral zone which has a second lining, passages in the second lining being smaller than passages in the first lining so that the pressure loss in the second lining is greater than that of the first lining. The second lining forms a sleeve surround the first lining and this sleeve is formed of at least one refractory heat insulating material. The oxidation reactor is provided with an external sleeve steel jacket, a concrete wall and a steel element surrounding the mixing member arranged above the reaction member.

Abstract: Method and apparatus for thermal conversion of methane to hydrocarbons of higher molecular weight, comprising a reactor 1 of elongated shape, connected at a first end to means 5 for supplying gas mixture containing methane (process gas), and connected at the opposite end to discharge means 10, the reactor having a plurality of electric heating means 3 surrounded by sheaths 4 over a first part (towards the first end). The heating means, which are substantially parallel, are arranged in sheets which are substantially parallel and perpendicular to the axis of the reactor, so that spaces or passages for circulation of the process gas and/or effluent are defined between the sheaths and/or between the sheaths and the walls 22 separating two consecutive sheets. The heating means are adapted to heat the passages by successive independent cross sections substantially perpendicular to the axis of the reactor.

Abstract: An oxidizable charge is oxidized in a gaseous phase reaction. The oxidizable charge and an oxidizing gas flow simultaneously and separately through a distribution zone made of a ceramic material. In at least a part of the distribution zone, the oxidizable charge and the oxidizing gas flow through a multiplicity of passages of a dimension so small that any flame resulting from oxidation of the oxidizable charge will be quenched. The oxidizable charge and oxidizing gas are then mixed in a mixing zone made from a ceramic material defining a multiplicity of spaces with passages having a dimension comparable to the dimension of the passages in the distribution zone. The mixture of gases then flows through a reaction zone made from a ceramic material defining another multiplicity of passages having dimensions comparable to those in the distribution zone.

Abstract: A process for thermally converting methane e.g., at 1,000.degree.-1,300.degree. C. into hydrocarbons with higher molecular weights, especially ethylene comprises circulating a gas containing methane in ceramic channels (11) grouped in rows which cover at least a part of the reactor (1) length, parallel to its axis. At the reaction temperature, the temperature variation is kept at less than 20.degree. C. The rows of channels form multiple plates (4) which are not adjacent to one another and which define tight spaces (17) in which are housed the electric heating (5, 22) means that heat the channel plates in a first zone (9) through successive, independent cross sections substantially perpendicular to the axis of the reactor and substantially parallel to the plane of the plates. Means for heating, servocontrol and modulation (7, 8) regulate the heating system. At the exit of the heating zone (9), the effluent is cooled in a second zone (10) equipped with cooling means and finally collected.