Abstract: A process for the recovery of ammonia contained in a gaseous stream is described, said process comprising the following phases: (a) subjecting the gaseous stream containing ammonia to a washing (S) with an aqueous washing solution (5a) having a pH lower than 7.0, with the formation of a purified gaseous stream (6) and an aqueous solution (7) containing an ammonium salt; (b) subjecting the aqueous solution containing the ammonium salt coming from phase (a) to a distillation process (MD) with a hydrophobic microporous membrane at a temperature ranging from 50 to 250° C. and a pressure ranging from 50 KPa to 4 MPa absolute with the formation of a regenerated washing solution (16) and a gaseous stream (18) comprising NH3 and H2O; (c) recycling said generated washing solution to phase (a). The equipment for carrying out the above process is also described.

Abstract: A process for the recovery of ammonia contained in a gaseous purging stream produced in a synthesis process of urea.

Abstract: A process for the recovery of ammonia contained in a gaseous stream is described, said process comprising the following phases: (a) subjecting the gaseous stream containing ammonia to a washing (S) with an aqueous washing solution (5a) having a pH lower than 7.0, with the formation of a purified gaseous stream (6) and an aqueous solution (7) containing an ammonium salt; (b) subjecting the aqueous solution containing the ammonium salt coming from phase (a) to a distillation process (MD) with a hydrophobic microporous membrane at a temperature ranging from 50 to 250° C. and a pressure ranging from 50 KPa to 4 MPa absolute with the formation of a regenerated washing solution (16) and a gaseous stream (18) comprising NH3 and H2O; (c) recycling said generated washing solution to phase (a). The equipment for carrying out the above process is also described.

Abstract: The present invention relates to a process for the recovery of ammonia contained in a gaseous purging stream produced in a synthesis process of urea, comprising the following phases: a) subjecting the gaseous purging stream to a washing with an aqueous acidic solution, at a pH ranging from 1 to 6, with the formation of a first purified gaseous stream and an aqueous solution containing an ammonium salt; b) subjecting the aqueous solution containing the ammonium salt coming from phase a) to stripping, after treatment with a strong base, at a temperature ranging from 50 to 250° C.

Abstract: Process for production of styrene by dehydrogenation of ethylbenzene in a reactor system comprising a dehydrogenation reactor and a fast riser catalyst regenerator.

Abstract: Process for the production of synthesis gas from heavy charges comprising a partial oxidation of heavy charges with oxygen or air enriched in oxygen in the presence of vapour, carried out at temperatures higher than 1000° C. and pressures equal to or higher than 20 atm and the subsequent cooling of the synthesis gas obtained, by the direct injection of water into the gas itself followed by the separation of the water effected by means of an adduction pipe surrounded by a concentric tube open at both ends so as to form a ring through which the cooled gas and water can rise, characterized in that the distance (L) between the lower end of the adduction pipe and the lower end of the open concentric tube must be equal to or higher than x times the diameter (D) of said lower end of the adduction pipe, wherein x varies in relation to the specific gas mass flow-rate (F), expressed in kg/h/cm2, according to the equation x=0.026 F+0.15.

Abstract: Integrated process for the production of alkyl and alkenyl substituted aromatic compounds which comprises simultaneously dehydrogentaing in a reactor-regenerator system a mixture containing an alkyl and an aromatic alkyl hydrocarbon coming from an alkylation unit and recycling the dehydrogenated alkyl hydrocarbon thus produced, after separation, to the alkylation unit.

Abstract: Reactor-regenerator device, comprising at least one reactor for catalytic dehydrogenation reactions of hydrocarbons and at least one regenerator of the catalyst of the “fast riser” type wherein the regenerator-riser is a substantially tubular apparatus for chemical reactions which comprise a gaseous phase in close contact with a solid phase, wherein gas phase and solid particles move upwards in co-current flow.

Abstract: Process for the production of synthesis gas from heavy charges comprising a partial oxidation of heavy charges with oxygen or air enriched in oxygen in the presence of vapour, carried out at temperatures higher than 1000° C. and pressures equal to or higher than 20 atm and the subsequent cooling of the synthesis gas obtained, by the direct injection of water into the gas itself followed by the separation of the water effected by means of an adduction pipe surrounded by a concentric tube open at both ends so as to form a ring through which the cooled gas and water can rise, characterized in that the distance (L) between the lower end of the adduction pipe and the lower end of the open concentric tube must be equal to or higher than x times the diameter (D) of said lower end of the adduction pipe, wherein x varies in relation to the specific gas mass flow-rate (F), expressed in kg/h/cm2, according to the equation x=0.026 F+0.15.

Abstract: Process for the production of synthesis gas, by means of catalytic partial oxidation or autothermal reforming of light hydrocarbons, which comprises partially oxidizing the hydrocarbon with oxygen coming from the reduction of at least one metal oxide selected from hexavalent chromium oxide, supported on an inert carrier and modified with an alkaline and/or earth-alkaline metal, and metal oxides capable of autonomously sustaining the catalytic partial oxidation reaction by means of redox cycles.

Abstract: Integrated process for the production of alkyl and alkenyl substituted aromatic compounds which comprises simultaneously dehydrogentaing in a reactor-regenerator system a mixture containing an alkyl and an aromatic alkyl hydrocarbon coming from an alkylation unit and recycling the dehydrogenated alkyl hydrocarbon thus produced, after separation, to the alkylation unit.

Abstract: An integrated process for producing iso-butene and alkyl tert-butyl ethers in which the iso-butene is obtained by dehydrogenation of iso-butane followed by purification by partial condensation plus absorption of residual vapor with a solvent, the alkyl tert-butyl ether being obtained by reacting the purified iso-butene product with the corresponding alcohol, the essential characteristic being that the solvent used for absorbing the iso-butene is part of the product alkyl tert-butyl ether itself and/or part of the corresponding alcohol used in the process.

Abstract: An integrated process for producing iso-butene and alkyl tert-butyl ethers in which the iso-butene is obtained by dehydrogenation of iso-butane followed by purification by partial condensation plus absorption of residual vapor with a solvent, the alkyl tert-butyl ether being obtained by reacting the purified iso-butene product with the corresponding alcohol, the essential characteristic being that the solvent used for absorbing the iso-butene is part of the product alkyl tert-butyl ether itself and/or part of the corresponding alcohol used in the process.