Process for separating butadiene from C4 hydrocarbons streams obtained by stream-cracking

Claim 2

A process for separating butadiene from C 4 hydrocarbon streams obtained by steam cracking containing, besides butadiene, C 4 linear saturated and olefinic hydrocarbons, isobutylene and acetylenic compounds characterized in that isobutylene is etherified in a first reactor with methanol or another alcohol in presence of an acid ion exchange resin, the acetylenic compounds are etherified with methanol or another alcohol in a second reactor in presence of the same or of different acid ion exchange resin containing mercuric ions in amount also lower than that of the acid ions and thereafter subjecting to distillation operations the ether containing mixture for separating both the saturated and olefinic hydrocarbons and said ethers from butadiene.

Claim 3

A process as claimed in claim 1 wherein the etherification of isobutylene and the etherification of the acetylenic compounds are carried out in the same reactor.

Claim 4

A process for separating butadiene from C 4 hydrocarbon streams obtained by steam cracking containing, besides butadiene, C 4 linear saturated and olefinic hydrocarbons, isobutylene and acetylenic compounds characterized in that 85% to 95% by weight of fed isobutylene is etherified with methanol in a first reactor in presence of an acid ion-exchange resin, the produced methyl ter-butyl ether is separated by distillation in a column, isobutylene remaining in the hydrocarbon stream and all acetylenic compounds in the same stream are then etherified with methanol in a second reactor in presence of an acid ion-exchange resin to which mercuric ions have been added, C 4 saturated and olefinic hydrocarbons are removed as overhead product from a subsequent extractive distillation column working with a solvent selective for butadiene and ethers, obtaining as bottom product a mixture of solvent, ethers and butadiene from which, by stripping in a column, butadiene is separated as overhead product, the ethers being discharged in vapour phase from an intermediate plate of the same column and sent again to the column effecting the separation of ter-butyl ether, the recovered solvent being utilized again in the extractive distillation column.

Claim 5

A process for separating butadiene from C 4 hydrocarbon streams obtained by steam cracking containing, besides butadiene, C 4 linear saturated and olefinic hydrocarbons, isobutylene and acetylenic compounds characterized in that 85% to 95% by weight of fed isobutylene is etherified with methanol in a first reactor in presence of an acid ion-exchange resin, the produced methyl ter-butyl ether is separated by distillation in a column, isobutylene remaining in the hydrocarbon stream and all acetylenic compounds in the same stream are then etherified with methanol in a second reactor in presence of an acid ion-exchange resin to which mercuric ions have been added, C 4 saturated and olefinic hydrocarbons are removed as overhead product from a subsequent extractive distillation column working with a solvent selective for butadiene and ethers, obtaining as bottom product a mixture of solvent, ethers and butadiene from which, by stripping in a column, butadiene is separated as overhead product, the ethers being discharged in vapour phase from an intermediate plate of the same column and sent again to the column effecting the separation of ter-butyl ether, the recovered solvent being utilized again in the extractive distillation column.

Claim 6

A process as claimed in claim 1 characterized in that the acid ion-exchange resin contains sulphonic groups (-SO 3 H).

Claim 7

A process as claimed in claim 1, characterized in that the acid ion-exchange resin contains carboxylic groups.

Claim 8

A process as claimed in claim 1 characterized in that the acid ion-exchange resin has polystyrene matrix.

Claim 9

A process as claimed in claim 1 characterized in that the acid ion-exchange resin has a polyphenolic matrix.

Claim 10

A process as claimed in claim 1 wherein the mercuric ions are added in the form of mercuric salts, particularly as mercury nitrate.

Claim 11

A process as claimed in claim 1 characterized in that the reaction in the first reactor is carried out at a temperature in the range of from 20° to 80° C with a working pressure at least equal to the vapour pressure of the feed mixture and LHSV in the range of from 2 to 30.

Claim 12

A process as claimed in claim 1 wherein the reaction in the second reactor is carried out in the range of from 20° to 80° C with a working pressure at least equal to the vapour pressure of the feed mixture and with LHSV in the range of from 1 to 30.

Claim 13

A process as claim in claim 3 wherein the separation of C 4 saturated and olefinic hydrocarbons is carried out by means of a liquid-liquid extraction column working with a solvent selective for butadiene and ethers.

Claim 14

A process as claimed in claim 3 wherein the solvent selective for butadiene and ethers is selected among N-formyl moropholine, N-methyl pyrrolidone, dimethylformamide, acetonitrile, dimethyl acetamide, N-methyl imidazole, 1,3 dimethyl imidazolydin 2 one and β-metoxypropionitrile.