Abstract: A phase change memory element includes a memory region, a first electrode and a second electrode. The memory region is arranged between the first and the second electrodes and is made of a GST alloy. An average percentage of germanium in the GST alloy is higher than 50%. The memory region has a storage portion formed by a GST alloy that includes nitrogen in an electrically relevant amount. The GST alloy of the storage portion has a percentage of germanium inclusively between 60% and 68%; a percentage of antimony inclusively between 9% and 5%; a percentage of tellurium inclusively between 18% and 10%; and a percentage of nitrogen inclusively between 5% and 25%.

Abstract: The invention concerns a petroleum product and a process for the production of a petroleum product which can form part of a blend for an internal combustion engine fuel, the process comprisinga) hydrotreating a hydrocarbon feedstock at a partial pressure of hydrogen at the reactor outlet of about 0.5 MPa to about 6 MPa,b) separating a product (P) from step a) into a product (P1) with a final boiling point of about 300.degree. C. and a product (P2) with an initial boiling point greater than the final boiling point of product (P1),c) performing a liquid-liquid extraction with a solvent (S1), to produce an extract (E1) and a raffinate (R1) from product (P2),d) recovering solvent (S1) from raffinate (R1) to produce a product (Q1), depleted in solvent (S1), which has improved qualities and contains less than 500 ppm by weight of sulphur.

Abstract: The invention concerns a petroleum product and a process for the production of a petroleum product which can form part of a blend for an internal combustion engine fuel, the process comprisinga) hydrotreating a hydrocarbon feedstock at a partial pressure of hydrogen at the reactor outlet of about 0.5 MPa to about 6 MPa,b) separating a product (P) from step a) into a product (P1) with a final boiling point of about 300.degree. C. and a product (P2) with an initial boiling point greater than the final boiling point of product (P1),c) performing a liquid-liquid extraction with a solvent (S1), to produce an extract (E1) and a raffinate (R1) from product (P2),d) recovering solvent (S1) from raffinate (R1) to produce a product (Q1), depleted in solvent (S1), which has improved qualities and contains less than 500 ppm by weight of sulphur.

Abstract: A fuel for internal combustion engines having an improved cetane index and lower sulfur content is obtained from a hydrocarbon charge, by a process comprising a step (a) for distillation (D1) in which a bottom product (Q1) is obtained via a line 3 and in which a top product (T1) is obtained via a line 2, a step (b) of liquid/liquid extraction (LE) using a solvent (S1) to obtain a raffinate (R1), (line 5) an extract from which product (Q1) is obtained (line 6), a step c) separating (D2) the raffinate (R1) enabling a product (Q2) to be obtained via line 7, which product has a low solvent (S1) content, and a step (d) of hydrotreatment (HDS) in which the mixture of the products (T1) and (Q2) are subjected to hydrotreatment with a hydrogen partial pressure of less than 10 megapascals, to obtain a product (P) (line 9) which has improved qualities and which contains less than 500 ppm by weight sulphur.

Abstract: A process for obtaining a fuel for internal combustion engines from a hydrocarbon charge, comprising a step (a) for distillation (D1) in which a bottom product (Q1) is obtained via a line 3 and in which a top product (T1) is obtained via a line 2, a step (b) of liquid/liquid extraction (LE) using a solvent (S1) to obtain a raffinate to (R1), (line 5) and an extract from which product (Q1) an extract (E1) is obtained (line 6) and a raffinate, a step c) of separating (D2) the raffinate (R1) enabling a product (Q2) to be obtained via line 7, which product has a low solvent (S1) content, and a step (d) of hydrotreatment (HDS) in which the mixture of the products (T1) and (Q2) are subjected to hydrotreatment with a hydrogen partial pressure of less than 10 megapascals, to obtain a product (P) (line 9) which has improved qualities and which contains less than 500 ppm by weight sulphur.

Abstract: A reactive distillation process which makes it possible, in the same enclosure, to carry out a catalytic reaction and isolate by distillation the sought product, in which the liquid phase containing the reagents passes from bottom to top through at least one catalyst bed, without the vapor phase of the distillation traversing said catalyst beds. These operating characteristics occur in a reactive distillation zone (C) including an alternation of distillation cells (D) having one or more trays (5) and reaction cells (R) containing the catalyst beds and designed in such a way that the liquid phase flowing from a distillation tray (5) flows above an overflow ( 7) through a downpipe (6) and approaches the base of the catalyst bed (8), traverses the latter in a downward flow and is then allowed to flow over a distillation tray (5) of the following distillation cell (D), so that the distillation vapor circulating from bottom to top through the distillation trays (5) does not traverse said reaction cells (R).

Abstract: For separating ETBE and ethanol the following principal stages are employed:(1) Extraction of ethanol by water, the raffinate being ETBE saturated in water and the extract an ethanol/water mixture containing a small proportion of ETBE;(2) Concentration of the above mixture, the distillate being a mixture close to the ethanol/water azeotrope in composition and containing a very small proportion of ETBE;(3) Heteroazeotropic distillation of this distillate in two coupled columns with an overhead decanter, this distillation using ETBE as azeotroping agent; the residue of the first column being ethanol which is ca. 99% by mole and the residue of the second column being practically pure water, this water and the water recovered during the concentration stage being used as extraction solvent in stage (1).Stage (3) may be an ethanol dehydration unit using ETBE as dehydrating agent.

Abstract: The separation of ethyl tertiobutyl ether from mixtures with ethanol is based on heteroazeotropic distillation with water as the entrainer using two distillation columns, coupled with an overhead decanter. Purified ethanol is collected from the bottom of the first column and purified ETBE from the bottom of the second column. The separation method may be incorporated into an ETBE production unit in which isobutene (contained in a C.sub.4 -cut from steam cracking, catalytic cracking, or dehydrogenation of isobutane) is etherified by ethanol. Ethanol separated from the ETBE is then recycled to the etherification zone.

Abstract: For the separation of tert. butyl ethyl ether from mixtures with ethanol, there are provided two distillation stages, the first being carried out at a pressure p.sub.1 equal to or higher than 1 bar, the second at a pressure p.sub.2 below p.sub.1 by a value .DELTA.p or 0.5 to 12 bars, p.sub.2 then being 0.5 to 10 bars. The second column distillate is partly supplied as reflux to the head of the second column and is in part recycled to the head of the first column. The purified TBEE is collected at the bottom of the first column and the purified ethanol at the bottom of the second column.This separation process can be integrated into a TBEE production unit comprising etherification by ethanol of the isobutylene contained in a C.sub.4 fraction from a catalytic cracking or steam cracking stage. The ethanol separated from the TBEE is then recycled to the etherification zone.