Abstract: The invention concerns a production method which consists in forming a reaction medium containing 2,2,4,4,-tetramethyl-3-pentanone, hydrogen peroxide, ammonia and a zeolitic structure catalyst and allowing the reaction to obtain said oxime. 2,2,4,4,-tetramethyl-3-pentanone and hydrogen peroxide can be obtained by auto-oxidation of 2,2,4,4,-tetramethyl-3-pentanol with oxygen or air. Hydroxylammonium salts are obtained by acid hydrolysis of said oxime.

Abstract: The ionic liquids according to the invention result from the reaction of a halogenated or oxyhalogenated Lewis acid based on titanium, niobium, tantalum, tin or antimony with an organic salt of formula X+A? in which A? is a halide anion and X+ a quaternary ammonium, quaternary phosphonium or ternary sulphonium cation. These liquids can be used in particular in the liquid-phase fluorination using HF of saturated or unsaturated compounds having C—Cl groups.

Abstract: Catalysts which are useful in the fluorination of halogenated hydrocarbons by HF in the gas phase are obtained by simple impregnation of a bulk chromium oxide with a solution of a nickel derivative, the chromium oxide used exhibiting a BET specific surface of greater than 150 m2/g and a pore volume of greater than 0.15 ml/g.

Abstract: The ionic liquids according to the invention result from the reaction of a halogenated or oxyhalogenated Lewis acid based on titanium, niobium, tantalum, tin or antimony with an organic salt of formula X+A− in which A− is a halide anion and X+ a quaternary ammonium, quaternary phosphonium or ternary sulphonium cation.

Abstract: Catalysts which are useful in the fluorination of halogenated hydrocarbons by HF in the gas phase are obtained by simple impregnation of a bulk chromium oxide with a solution of a nickel derivative, the chromium oxide used exhibiting a BET specific surface of greater than 150 m2/g and a pore volume of greater than 0.15 ml/g.

Abstract: Azines, e.g., ketazines, are continuously produced by (i) establishing a loop having an azine reaction medium circulating therein, such loop including an azine reaction zone, means for separating azine final product from the circulating reaction medium, means for heating the reaction medium and for purging water therefrom, and means for recycling heated and purged reaction medium to the azine reaction zone, (ii) introducing hydrogen peroxide, ammonia and a carbonyl compound into the circulating reaction medium in the azine reaction zone, (iii) withdrawing azine final product thus formed from the circulating reaction medium. downstream of the azine reaction zone, (iii) thereafter purging water from the circulating reaction medium to maintain the volume thereof essentially constant, (iv) heating the circulating reaction medium to a temperature of at least 130° C.

Abstract: The invention concerns a method for preparing methyl ethyl ketone azine which consists in: (a) reacting ammonia, hydrogen peroxide and methyl ethyl ketone in the presence of a working solution to form an azine; (b) separating the working solution and the azine possibly containing methyl ethyl ketone which has not reacted and butanol-2; (c) recycling the working solution to step (a) after optional treatment; (d) separating the methyl ethyl ketone and the butanol-2 from the azine. The butanol-2 of the flow in step (d) is either purged or dehydrogenated in MEK and recycled at step (a).

Abstract: The invention concerns a method for making hydrazine hydrate which consists in hydrolyzing methyl ethyl ketone azine to obtain hydrazine hydrate and methyl ethyl ketone, characterised in that it consists in purging heterocyclic compounds of the pyrazoline family to prevent coloration of the hydrazine hydrate.

Abstract: A method for preparing hydrazine hydrate comprising: (a) reacting ammonia, hydrogen peroxide and methyl ethyl ketone in a working solution to form an azine; (b) separating the working solution from a mixture comprising the azine, methyl ethyl ketone oxime and optionally the methyl ethyl ketone which had not reacted; (c) recycling the working solution to step (a) after an optional treatment; (d) hydrolyzing the azine to obtain hydrazine hydrate and regenerating the methyl ethyl ketone; (e) recycling to step (a) the methyl ethyl ketone. In step (d) the methyl ethyl ketone oxime is purged.

Abstract: Catalysts which are useful in the fluorination of halogenated hydrocarbons by HF in the gas phase are obtained by simple impregnation of a bulk chromium oxide with a solution of a nickel derivative, the chromium oxide used exhibiting a BET specific surface of greater than 150 m2/g and a pore volume of greater than 0.15 ml/g.

Abstract: An improved method for the selective vapor phase oxidation of acrolein to acrylic acid in a recirculating solids reactor system using a particulate molybdenum vanadate multimetal oxide as oxidant involving specific reactant concentrations (preferably 5 mol % to 30 mol % propylene, 0 to 20 mol % oxygen, 0 to 70 mol % water, and the remainder inert gas), solids particle size (20 to 300 micrometers), temperature (250 to 450° C.) and gas (1 to 15 seconds) and solids (2 to 60 seconds) residence times. Such a process leads to improved selectivity, conversion and solids conversion ratio.

Abstract: Solid mixed oxides composition of formula (I):

Abstract: A mixed oxide solid composition of the formulas (I): (a) Mo12Co4.7Bi1Ni2.6Fe3.7W0.5Sn0.5Si1K0.08Ox; (b) Mo12Co3.5Bi1.1Fe0.8W0.5Si1.4K0.05Ox; and (c) Mo12Co3.8Bi1.2Fe0.9W1.1Si1.5K0.05Ox, wherein x is the quantity of oxygen bonded to the other elements and depends on their oxidation states, is suitable for the manufacture of acrolein by oxidizing propylene. The solid composition reacts with propylene according to the redox reaction (1): solidoxidized+propylene→solidreduced+acrolein  (1) To manufacture acrolein, gaseous propylene is passed over the solid composition. Redox reaction (1) is conducted at a temperature of 200 to 600° C., at a pressure of 1.01×104 to 1.01 to 106 Pa (0.1 to 10 atmospheres) and with a residence time of 0.01 second to 90 seconds, in the absence of molecular oxygen.

Abstract: A mixed oxide solid composition of formula (I):Mo.sub.12 W.sub.a Bi.sub.b Fe.sub.c Co.sub.d Ni.sub.e Si.sub.f K.sub.g Sn.sub.h O.sub.x (I)where O.ltoreq.a.ltoreq.5, 0.5.ltoreq.b.ltoreq.5, 0.1.ltoreq.c.ltoreq.10, 0.5.ltoreq.d.ltoreq.10, 0.ltoreq.e.ltoreq.10, 0.ltoreq.f.ltoreq.15, 0.ltoreq.g.ltoreq.1, 0.ltoreq.h.ltoreq.2 and x is the quantity of oxygen bonded to the other elements and depends on their oxidation states, is used in the manufacture of acrolein by oxidizing propylene, the solid composition reacting with propylene according to the redox reaction (1):solid.sub.oxidized +propylene.fwdarw.solid.sub.reduced +acrolein(I)To manufacture acrolein, gaseous propylene is passed over a solid composition of formula (I), to conduct the redox reaction (1) by operating at a temperature of 200 to 600.degree. C., at a pressure of 1.01.times.10.sup.4 to 1.01 to 10.sup.6 Pa (0.1 to 10 atmospheres) and with a residence time of 0.01 second to 90 seconds, in the absence of molecular oxygen.

Abstract: Solid mixed oxides composition of formula (I):Mo.sub.12 V.sub.a Sr.sub.b W.sub.c Cu.sub.d Si.sub.e O.sub.x(I)2.ltoreq.a.ltoreq.14, 0.1.ltoreq.B.ltoreq.6, 0.ltoreq.c.ltoreq.12, 0.ltoreq.d.ltoreq.6, 0.ltoreq.e.ltoreq.15; x is the quantity of oxygen bonded to the other elements and depends on their oxidation states, are used in the manufacture of acrylic acid by oxidation of acrolein, the said solid composition reacting with acrolein according to the redox reaction (1):SOLID.sub.oxidized +ACROLEIN.fwdarw.SOLID.sub.reduced +ACRYLIC ACID(1).To manufacture acrylic acid, a gaseous mixture of acrolein and of water vapor and, if appropriate, of an inert gas is passed over a solid composition of formula (I), to conduct the redox reaction (1) by operating at a temperature of 200 to 500.degree. C., at a pressure of 1.01.times.10.sup.4 to 1.01.times.10.sup.6 Pa (0.1 to 10 atmospheres), and with a residence time of 0.01 second to 90 seconds, in the absence of molecular oxygen.

Abstract: A process of dignifying lignocellulosic pulp with oxygen followed by treatment of the delignified pulp with a chelating agent, followed by washing, followed by treatment with hydrogen peroxide at an alkaline pH in the presence of an alkali metal silicate at a temperature greater than 100.degree. C. and a pressure greater than 1.5 times the saturated vapor pressure.

Abstract: In order to purify a crude pentafluoroethane (F125) containing chloropentafluoroethane (F115), it is subjected to a heat treatment in the presence of hydrogen, the treatment being carried out at a temperature at least equal to 550.degree. C. and with an H.sub.2 /F115 molar ratio of at least 10.

Abstract: The present invention relates to the simultaneous manufacture of difluoromethane (F32) and 1,1,1,2-tetrafluoroethane (F134a) by pyrolysis of chlorodifluoromethane in the presence of hydrogen, working at a temperature above 500.degree. C. in the absence of any catalyst or metal surface. Depending on the operating conditions chosen, this process also makes it possible predominantly to manufacture either F134a or F32.

Abstract: Process for synthesizing 1,1,1-trifluoroethane (143a) in the gaseous phase by reacting 1,1-defluoro-1-chloroethane in gaseous phase in the presence of a Cr catalyst. The process may be run isothermally or adiabatically, without co-feeding air or other oxygen containing gas, in the presence or absence of a Ni, Co, Zn or Mn cocatalyst for the Cr catalyst. The catalyst may be unsupported or supported with a support preferably selected from activated carbon, alumina and fluorided alumina. The formation of olefin byproduct can be kept to less than 10 ppm in accordance with the process of the invention.

Abstract: The subject of the invention is a continuous process for the preparation of 1,1,1,2-tetrafluoroethane (134a) from 2-chloro-1,1,1-trifluoroethane (133a) and hydrofluoric acid in the gaseous phase in the presence of a chromium-based catalysts.According to the invention, the flow of gas leaving the reactor is subjected to a distillation in order to separate at the top a flow containing almost all the HC1 and at least 90% of the 134a produced by the reaction and at the bottom a flow containing at least 90% of the unconverted reactants (133a and HF), and the latter flow is recycled directly to the reactor, without any purifying operation.