KR930017847A - Selective Hydrogenation Process of Diolephine - Google Patents

Abstract

The selective hydrogenation of the diolefins contained in the purified C ₅ stream, in which the catalyst used is also a component of the distillation structure, essentially does not protect the monoolefins. In addition, some monoolefins can be isomerized to more useful monoolefin isomers.

Description

Selective Hydrogenation Process of Diolefin

Since this is an open matter, no full text was included.

1 is a simplified work flow diagram of the first embodiment of the present invention. 2 is a simplified working flowchart of the second embodiment of the present invention. 3 is a simplified working flowchart of the third embodiment of the present invention. 4 is a simplified working flowchart of the fourth embodiment of the present invention.

Claims (15)

A selective hydrogenation process of diolephine contained in hard naphtha, consisting of the following steps; (a) feeding a first flow consisting of light naphtha containing (1) diolefins and (2) a second flow containing hydrogen to a distillation column reactor as a feed zone; (b) reacting essentially all of the diolefin with the hydrogen by contacting (i) the first and second streams with a hydrogenation catalyst which can act as a distillation structure in the distillation reaction zone simultaneously in the distillation column reactor. Forming pentene and other hydrogenation products at and (ii) operating the pressure of the distillation column reactor such that the temperature of the distillation reaction zone is in the selected range and a portion of the mixture is vaporized by exothermic reaction; (c) step (b) withdrawing the liquid portion from (ii) from the distillation column reactor as bottoms; And (d) withdrawing the vapor portion from step (b) (ii) as overhead from the distillation column reactor with any unreacted hydrogen. The process of claim 1, wherein the overhead is cooled to condense any condensable material and to separate the condensable material from the unreacted hydrogen and return as reflux to the upper portion of the distillation column. 3. The process of claim 2 wherein the vapor portion from step (b) contains substantially all C ₅ and lighter boiling fractions and the liquid from step (b) contains substantially all C ₅ and heavier boiling fractions. And the condensable material comprises C ₅ . The process of claim 3, wherein a portion of the condensable material is withdrawn as distillation product. The process of claim 2 wherein the separated hydrogen is recycled to the distillation column reactor. The hydrogenation catalyst of claim 1, wherein the hydrogenation catalyst is composed of 0.34% by weight palladium oxide supported on a 1/8 inch (0.3175 cm) alumina sphere. Forming and stopping in the distillation column reactor. The process of claim 1, wherein hydrogen is contained in the second stream in an amount that provides a molar ratio of 1: 1 to 2: 1 of hydrogen to the diolefin. The process of claim 1 wherein the overhead pressure of the distillation column reactor is between 0 and 250 psig. The process of claim 8, wherein the temperature in the distillation reaction zone is between 37.8 ° C. (100 ° F.) and 148.9 ° C. (300 ° F.). 10. The process of claim 9 wherein the temperature in the distillation reaction zone is between 37.8 ° C. (100 ° F.) and 148.9 ° C. (300 ° F.), wherein the pentene consists of 3-methylbutene-1 and 2-methylbutene-2, A portion of said 3-methylbutene-1 isomerized to 2-methyl butene-2. The process of claim 1 wherein the distillation product containing C ₅ is withdrawn as a side stream below the top of the distillation column reactor. Selective hydrogenation of the diolefins and isomerization of monoolefins in light naphtha consisting of the following steps: (a) (1) 3-methylbutene-1, 2-methylbutene-1, 2 consisting of light naphtha Distillation column for the first flow containing methylbutene-2, 2-methyl butadiene-1, 3, cis 1, 3-pentadiene and trans 1,3-pentadiene and (2) the second flow containing hydrogen Feeding the reactor to the feed zone; (b) at the same time in the distillation column reactor (i) contacting the first and second streams with a hydrogenation catalyst which acts as a distillation structure in the distillation reaction zone, thereby essentially all of the above 2 -Methylbutadiene, cis 1, 3-pentadiene and trans 1, 3-pentadiene are reacted with the hydrogen to form pentene and isomerization of a portion of the 3-methylbutene-1 to 2-methylbutene in the reaction mixture Forming 2, and (ii) reducing the overhead pressure of the distillation column reactor to about 200 p. adjusting to a pressure of sig such that the temperature of the mixture in the distillation reaction zone is 121.1 ° C. (250 ° F.)-132.2 ° C. (270 ° F.) and a portion of the mixture is vaporized by exothermic reaction; (c) withdrawing the liquid portion from step (b) (ii) from the distillation column reactor as a bottom; And (d) withdrawing the vapor portion from step (b) (ii) as overhead from the distillation column reactor with any unreacted hydrogen. 13. The process of claim 12, wherein the overhead is cooled to condense any condensable material and to separate the condensable material from the unreacted hydrogen and return as reflux to the upper portion of the distillation column. The process of claim 13, wherein the separated hydrogen is recycled to the distillation column reactor. Selective hydrogenation process of diolefins contained in light naphtha, consisting of the following steps: (a) (1) a first flow consisting of light naphtha containing diolefin and (2) a second flow containing hydrogen Supplying a distillation column reactor to a feed zone; (b) at the same time in the distillation column reactor (i) palladium oxide supported on alumina particles, comprising (i) the first and second flows in a pocket of a fabric belt which twists with a distillation wire in a distillation reaction zone to form a catalytic distillation structure. Reacting essentially all of the diolefin with the hydrogen to form pentene and other hydrogenation products in the reaction mixture by contacting a hydrogenation catalyst consisting of, and (ii) the overhead pressure of the distillation column reactor in the range of 130 to 210 psig. Adjusting the temperature of the distillation zone to 110.0 ° C. (230 ° F.) to 132.2 ° C. (270 ° F.) and evaporating a portion of the mixture by exothermic reaction; (c) from step (b) (ii) Withdrawing the first liquid portion from the distillation column reactor as a bottoms; (d) withdrawing the second liquid portion from step (b) as a side stream; (e) any unreacted hydrogen Together withdrawing the vapor portion from step (b) (ii) as overhead from the distillation column reactor; (f) all compounds which cool the overhead and condense at that temperature and the overhead pressure between 130 and 210 psig (G) separating the condensed material from any uncondensed material at the overhead and returning a portion of the condensed material to the distillation column reactor as reflux; (h) the condensed material Withdrawing the remaining portion of the product as a distillation product; And (i) recycling any unreacted hydrogen confined to the uncondensed material to the distillation column reactor. ※ Note: The disclosure is based on the initial application.