Provided is a method for producing 1,3-butadiene that enables 1,3-butadiene to be obtained in a high yield while preventing abnormal reaction of a fraction containing vinylacetylene in high concentration. The method for producing 1,3-butadiene is a method for producing 1,3-butadiene from a fraction produced in separation and recovery of 1,3-butadiene from a C.sub.4 hydrocarbon mixture that includes: adding a diluent to a high VA fraction containing vinylacetylene to produce a diluted fraction; and subjecting the diluted fraction to hydrogenation treatment to produce 1,3-butadiene. Substantially only a low VA fraction is used as the diluent. The low VA fraction is a fraction that is produced in separation and recovery of 1,3-butadiene from the C.sub.4 hydrocarbon mixture and has a lower vinylacetylene concentration than the high VA fraction.

Provided is a method for producing 1,3-butadiene that enables 1,3-butadiene to be obtained in a high yield while preventing abnormal reaction of a fraction containing vinylacetylene in high concentration. The method for producing 1,3-butadiene is a method for producing 1,3-butadiene from a fraction produced in separation and recovery of 1,3-butadiene from a C.sub.4 hydrocarbon mixture that includes: adding a diluent to a high VA fraction containing vinylacetylene to produce a diluted fraction; and subjecting the diluted fraction to hydrogenation treatment to produce 1,3-butadiene. Substantially only a low VA fraction is used as the diluent. The low VA fraction is a fraction that is produced in separation and recovery of 1,3-butadiene from the C.sub.4 hydrocarbon mixture and has a lower vinylacetylene concentration than the high VA fraction.

Provided is a method for producing 1,3-butadiene that enables 1,3-butadiene to be obtained in a high yield while preventing abnormal reaction of a fraction containing vinylacetylene in high concentration. The method for producing 1,3-butadiene is a method for producing 1,3-butadiene from a fraction produced in separation and recovery of 1,3-butadiene from a C.sub.4 hydrocarbon mixture that includes: adding a diluent to a high VA fraction containing vinylacetylene to produce a diluted fraction; and subjecting the diluted fraction to hydrogenation treatment to produce 1,3-butadiene. Substantially only a low VA fraction is used as the diluent. The low VA fraction is a fraction that is produced in separation and recovery of 1,3-butadiene from the C.sub.4 hydrocarbon mixture and has a lower vinylacetylene concentration than the high VA fraction.

A process for the preparation of a catalyst comprising palladium, a porous support with a specific surface area in the range 140 to 250 m.sup.2/g, said catalyst being prepared by a process comprising the following steps: a) preparing a colloidal solution of palladium oxide or palladium hydroxide in an aqueous phase; b) adding said solution obtained from step a) to said porous support at a flow rate in the range 1 to 20 litre(s)/hour; said porous support being contained in a rotary impregnation device functioning at a rotational speed in the range 10 to 20 rpm; c) optionally, submitting the impregnated porous support obtained from step b) to a maturation; d) drying the catalyst precursor obtained from step b) or c); e) calcining the catalyst precursor obtained from step d).

A process for the preparation of a catalyst comprising palladium, a porous support with a specific surface area in the range 140 to 250 m.sup.2/g, said catalyst being prepared by a process comprising the following steps: a) preparing a colloidal solution of palladium oxide or palladium hydroxide in an aqueous phase; b) adding said solution obtained from step a) to said porous support at a flow rate in the range 1 to 20 litre(s)/hour; said porous support being contained in a rotary impregnation device functioning at a rotational speed in the range 10 to 20 rpm; c) optionally, submitting the impregnated porous support obtained from step b) to a maturation; d) drying the catalyst precursor obtained from step b) or c); e) calcining the catalyst precursor obtained from step d).

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a variety of methods for starting up reactors for use in methods for selectively hydrogenating acetylene using a catalyst composition comprises a porous support, palladium, and one or more ionic liquids.

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a variety of methods for starting up reactors for use in methods for selectively hydrogenating acetylene using a catalyst composition comprises a porous support, palladium, and one or more ionic liquids.