The present invention relates to a process for treating an effluent obtained from an oligomerization step in a vaporization step. In particular, the oligomerization step is a step for dimerization of ethylene to 1-butene with a nickel-based catalytic system.

The present invention relates to a process for treating an effluent obtained from an oligomerization step in a vaporization step. In particular, the oligomerization step is a step for dimerization of ethylene to 1-butene with a nickel-based catalytic system.

Systems and processes disclosed may be used to produce a high purity isobutane stream and a high purity 1-butene stream from mixed C4 streams having disparate starting compositions.

Systems and processes disclosed may be used to produce a high purity isobutane stream and a high purity 1-butene stream from mixed C4 streams having disparate starting compositions.

Processes for producing olefins include integration of steam cracking with a dual catalyst metathesis process. The processes include steam cracking a hydrocarbon feed to form a cracking reaction effluent containing butenes, separating the cracking reaction effluent to produce a cracking C4 effluent including normal butenes, isobutene, and 1,3-butadiene, subjecting the cracking C4 effluent to selective hydrogenation to convert 1,3-butadiene in the cracking C4 effluent to normal butenes, removing isobutene from a hydrogenation effluent to produce a metathesis feed containing normal butenes, and contacting the metathesis feed with a metathesis catalyst and a cracking catalyst directly downstream of the metathesis catalyst to produce a metathesis reaction effluent. Contacting with the metathesis catalyst causes metathesis of normal butenes to produce ethylene, propene, and C5+ olefins, and contacting with the cracking catalyst causes C5+ olefins produced through metathesis to undergo cracking reactions to produce additional propene, ethylene, or both.

Processes for producing olefins include integration of steam cracking with a dual catalyst metathesis process. The processes include steam cracking a hydrocarbon feed to form a cracking reaction effluent containing butenes, separating the cracking reaction effluent to produce a cracking C4 effluent including normal butenes, isobutene, and 1,3-butadiene, subjecting the cracking C4 effluent to selective hydrogenation to convert 1,3-butadiene in the cracking C4 effluent to normal butenes, removing isobutene from a hydrogenation effluent to produce a metathesis feed containing normal butenes, and contacting the metathesis feed with a metathesis catalyst and a cracking catalyst directly downstream of the metathesis catalyst to produce a metathesis reaction effluent. Contacting with the metathesis catalyst causes metathesis of normal butenes to produce ethylene, propene, and C5+ olefins, and contacting with the cracking catalyst causes C5+ olefins produced through metathesis to undergo cracking reactions to produce additional propene, ethylene, or both.

Mixed pentenes may be converted to propylene by feeding an alcohol, linear pentenes, and isopentenes to an etherification reactor. The alcohol and isopentenes may be reacted in the etherification reactor to convert isopentenes to tertiary amyl alkyl ether, which may be separated from the linear pentenes, recovered as a linear pentene fraction. The tertiary amyl alkyl ether may be fed to a decomposition reactor to convert at least a portion of the tertiary amyl alkyl ether to alcohol and isopentenes. The alcohol and isopentenes may then be separated to recover an isopentene fraction and an alcohol fraction. The isopentene fraction is then fed to a skeletal isomerization reactor to convert at least a portion of the isopentenes to linear pentenes, the effluent from which may be recycled to the etherification reactor. Ethylene and the linear pentene fraction may then be fed to a metathesis reactor to produce propylene.

Mixed pentenes may be converted to propylene by feeding an alcohol, linear pentenes, and isopentenes to an etherification reactor. The alcohol and isopentenes may be reacted in the etherification reactor to convert isopentenes to tertiary amyl alkyl ether, which may be separated from the linear pentenes, recovered as a linear pentene fraction. The tertiary amyl alkyl ether may be fed to a decomposition reactor to convert at least a portion of the tertiary amyl alkyl ether to alcohol and isopentenes. The alcohol and isopentenes may then be separated to recover an isopentene fraction and an alcohol fraction. The isopentene fraction is then fed to a skeletal isomerization reactor to convert at least a portion of the isopentenes to linear pentenes, the effluent from which may be recycled to the etherification reactor. Ethylene and the linear pentene fraction may then be fed to a metathesis reactor to produce propylene.

The present invention relates to a process for treating, by reactive distillation, an olefinic feedstock comprising linear olefins containing n carbon atoms, and branched olefins, the branched olefins comprising tertiary branched olefins, for example a mixture of n-butenes and of tertiary branched olefins comprising isobutene, so as to produce an olefinic effluent with a mass content of tertiary branched olefin of less than or equal to 3% by weight and a heavy hydrocarbon effluent, said process comprising the feeding of a reactive distillation section with said olefinic feedstock and with an alcohol feedstock comprising a primary alcohol, said reactive distillation section comprising a column composed at least of an upper reflux zone into which is introduced said alcohol feedstock, comprising, for example, ethanol, an intermediate reaction zone comprising at least 6 reactive doublets, and a lower fractionation zone at the level of which said section is fed with said olefinic feedstock, said reactive distillation section being operated at a relative pressure of between 0.3 and 0.5 MPa, a column head temperature of between 40° C. and 60° C., with a reflux ratio of between 1.8 and 2.2.

The present invention relates to a process for treating, by reactive distillation, an olefinic feedstock comprising linear olefins containing n carbon atoms, and branched olefins, the branched olefins comprising tertiary branched olefins, for example a mixture of n-butenes and of tertiary branched olefins comprising isobutene, so as to produce an olefinic effluent with a mass content of tertiary branched olefin of less than or equal to 3% by weight and a heavy hydrocarbon effluent, said process comprising the feeding of a reactive distillation section with said olefinic feedstock and with an alcohol feedstock comprising a primary alcohol, said reactive distillation section comprising a column composed at least of an upper reflux zone into which is introduced said alcohol feedstock, comprising, for example, ethanol, an intermediate reaction zone comprising at least 6 reactive doublets, and a lower fractionation zone at the level of which said section is fed with said olefinic feedstock, said reactive distillation section being operated at a relative pressure of between 0.3 and 0.5 MPa, a column head temperature of between 40° C. and 60° C., with a reflux ratio of between 1.8 and 2.2.