Process and apparatus for the preparation of ether

Claim 2

In a process for the production of tertiary alkyl methyl ether (TAME) comprising etherifying a C 5 olefin-containing hydrocarbon feed stream with methyl alcohol in a reactor; fractionally distilling resultant reaction product formed during the etherifying into an overhead fraction containing essentially unreacted hydrocarbons and unreacted alcohol, and a bottom fraction containing essentially the ether; condensing the overhead fraction; and separating the alcohol from the condensed overhead fraction, the improvement which comprises cooling the condensed overhead fraction to below the single phase saturation temperature to form immiscible liquid phases, one containing essentially the alcohol and the other containing essentially the hydrocarbons, and withdrawing the immiscible phases separately from each other, with the provision that water is not added in said separating step to separate the alcohol from the C 5 hydrocarbon so as to form an aqueous phase containing the alcohol which is thereafter distilled into water and alcohol fractions.

Claim 3

A process according to claim 1 further comprising recycling at least part of the withdrawn immiscible phase containing essentially the alcohol into the etherification reactor.

Claim 4

A process according to claim 1 wherein said cooling of the overhead fraction is conducted in indirect heat exchange with a cold stream from a low-temperature gas separation facility.

Claim 5

A process according to claim 1 wherein said cooling of the overhead fraction, prior to separation of the two phases, is conducted to a temperature of -60° to +50° C.

Claim 6

A process according to claim 1 further comprising admixing a minor amount of water to the overhead fraction prior to phase separation in order to increase the separability of the immiscible phases, most of said water being passed into the liquid phase containing essentially alcohols and the remainder of said water passing into said liquid phase containing essentially the hydrocarbons.

Claim 7

A process according to claim 5 wherein the admixed proportion of water is between 0.01 and 2% by weight of the overhead fraction.

Claim 8

A process according to claim 5 further comprising recycling at least part of the withdrawn immiscible phase containing essentially the methyl alcohol into the etherification reactor without removing said water from said immiscible phase in an interventing step.

Claim 9

A process according to claim 5 further comprising passing at least a portion of the immiscible phase containing essentially the hydrocarbons directly into the fractional distillation zone as reflux liquid.

Claim 10

A process according to claim 8, wherein said cooling of the overhead fraction, prior to separation of the two immiscible phases, ranges to temperatures of about -43 ° to -60° C.

Claim 11

A process according to claim 1 wherein the distillation and the phase separation are conducted under a pressure of 1-20 bar.

Claim 12

A process according to claim 1 further comprising combining at least a portion of the immiscible phase containing essentially the hydrocarbons with withdrawn bottoms fraction from the fractional distillation step.

Claim 13

A process according to claim 1 further comprising passing at least a portion of the immiscible phase containing essentially the hydrocarbons directly into the fractional distillation zone as reflux liquid.

Claim 14

A process according to claim 1 wherein the feed stream is a light gasoline fraction from a thermal or catalytic cracking stage.

Claim 15

A process according to claim 1, wherein the bottoms fraction of the distillation column contains the ether in a mixture with a portion of the unreacted hydrocarbons.

Claim 16

A process according to claim 1 wherein the etherification is conducted at a temperature of +40° to -120° C. and under an absolute pressure of 1.2-20 bar.

Claim 17

A process according to claim 1, wherein said cooling of the overhead fraction, prior to separation of the two immiscible phases, ranges to temperatures of about -43° to -60° C.

Claim 18

A process according to claim 1, wherein distillation and phase separation are conducted under a pressure of about 1.5-3 bar.

Claim 19

A process according to claim 1, further comprising separating the ether from the bottoms fraction of the distillation.

Claim 20

A process according to claim 1, wherein at least part of the heat reaction liberated during etherification is employed to heat up at least a portion of the hydrocarbon feed stream passed into the reactor.

Claim 21

In a process for the production of tertiary amyl methyl ether (TAME) comprising etherifying an olefin-containing, essentially C 5 hydrocarbon feed stream with methyl alcohol in a reactor; fractionally distilling resultant reaction product formed during the etherifying into an overhead fraction containing essentially unreacted hydrocarbons and unreacted methyl alcohol and a bottom fraction containing essentially the ether; condensing the overhead fraction; and separating the methyl alcohol from the condensed overhead fraction, the improvement which comprises cooling the condensed overhead fraction to below the single phase saturation temperature to form only two immiscible liquid phases, one containing essentially the methyl alcohol and the other containing essentially the hydrocarbons, and withdrawing the immiscible phases separately from each other with the provision that water in a proportion of between 0.01 and 2% by weight of the overhead fraction is admixed to the overhead fraction prior to phase separation, said water providing increased separability of the two immiscible phases and most of the water transferring into the methanol phase upon condensation, said water being present in said methanol phase in a substantially smaller weight proportion compared to the methanol.

Claim 22

In a process for the production of tertiary amyl methyl ether (TAME) comprising etherifying an olefin-containing, essentially C 5 hydrocarbon feed stream with methyl alcohol in a reactor; fractionally distilling resultant reaction product formed during the etherifying into an overhead fraction containing essentially unreacted hydrocarbons and unreacted methyl alcohol and a bottom fraction containing essentially the ether; condensing the overhead fraction; and separating the methyl alcohol from the condensed overhead fraction, the improvement which comprises cooling the condensed overhead fraction to below the single phase saturation temperature to form only two immiscible liquid phases, one containing essentially the methyl alcohol and the other containing essentially the hydrocarbons, and withdrawing the immiscible phases separately from each other with the provision that water in a proportion of between 0.01 and 2% by weight of the overhead fraction is admixed to the overhead fraction prior to phase separation, said water providing increased separability of the two immiscible phases and most of the water transferring into the methanol phase upon condensation, said water being present in said methanol phase in a substantially smaller weight proportion compared to the methanol.