A process for producing an organic compound using a flow reactor for a first reaction in which a raw material liquid A and a raw material liquid B are mixed, and reacted in a reactor unit, and a flow reactor for a second reaction in which a first reaction solution discharged from the flow reactor for the first reaction and a raw material liquid C are mixed, and reacted in a reactor unit, wherein the raw material liquid A is a solution in which triphosgene and/or diphosgene is dissolved, wherein the raw material liquid B is a nitrogen-containing organic compound or a solution thereof, wherein the raw material liquid C is a reaction substrate having a functional group capable of reacting with phosgene, or a solution containing the reaction substrate, and wherein a product of the first reaction is phosgene.

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction.

A process for converting an anhydrous off-gas stream from melamine synthesis plants to urea and the relative plant for the direct conversion of an anhydrous off-gas stream from melamine synthesis plants into urea, are described.

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction.

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction.

A process for producing an organic compound using a flow reactor for a first reaction in which a raw material liquid A and a raw material liquid B are mixed, and reacted in a reactor unit, and a flow reactor for a second reaction in which a first reaction solution discharged from the flow reactor for the first reaction and a raw material liquid C are mixed, and reacted in a reactor unit, wherein the raw material liquid A is a solution in which triphosgene and/or diphosgene is dissolved, wherein the raw material liquid B is a nitrogen-containing organic compound or a solution thereof, wherein the raw material liquid C is a reaction substrate having a functional group capable of reacting with phosgene, or a solution containing the reaction substrate, and wherein a product of the first reaction is phosgene.

The present invention relates to an integrated process to convert crude oil into petrochemical products comprising crude oil distillation, hydrocracking and olefins synthesis, which process comprises subjecting a hydrocracker feed to hydrocracking to produce LPG and BTX and subjecting the LPG produced in the process to olefins synthesis. Furthermore, the present invention relates to a process installation to convert crude oil into petrochemical products comprising: a crude distillation unit comprising an inlet for crude oil and at least one outlet for one or more of naphtha, kerosene and gasoil; a hydrocracker comprising an inlet for a hydrocracker feed, an outlet for LPG and an outlet for BTX; and a unit for olefins synthesis comprising an inlet for LPG produced by the integrated petrochemical process installation and an outlet for olefins. The hydrocracker feed used in the process and the process installation of the present invention comprises one or more of naphtha, kerosene and gasoil produced by crude oil distillation in the process; and refinery unit-derived light-distillate and/or refinery unit-derived middle-distillate produced in the process. The process and process installation of the present invention have an increased production of petrochemicals at the expense of the production of fuels and an improved carbon efficiency in terms of the conversion of crude oils into petrochemicals.

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction.

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit.

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit.