A method for processing pentanes obtained from a DIB unit is disclosed. The process can include separating a first stream containing pentanes obtained from a DIB unit, in a separation column to obtain a second stream comprising iso-pentane and a third stream comprising n-pentane and neo-pentane; and subjecting the third stream to a butane isomerization unit producing a fourth stream containing iso-pentane, n-pentane, and neo-pentane.

A method for processing pentanes obtained from a DIB unit is disclosed. The process can include separating a first stream containing pentanes obtained from a DIB unit, in a separation column to obtain a second stream comprising iso-pentane and a third stream comprising n-pentane and neo-pentane; and subjecting the third stream to a butane isomerization unit producing a fourth stream containing iso-pentane, n-pentane, and neo-pentane.

Provided is a separation membrane that is suitable for use in separating one or more hydrocarbons from a hydrocarbon mixture. More specifically, the separation membrane includes a porous support for which acid content is not substantially detected by ammonia temperature programmed desorption in a temperature range of higher than 450° C. and not higher than 600° C. and a porous separation layer containing a zeolite that is disposed on the porous support.

Provided is a separation membrane that is suitable for use in separating one or more hydrocarbons from a hydrocarbon mixture. More specifically, the separation membrane includes a porous support for which acid content is not substantially detected by ammonia temperature programmed desorption in a temperature range of higher than 450° C. and not higher than 600° C. and a porous separation layer containing a zeolite that is disposed on the porous support.

Provided is a separation membrane that is suitable for use in separating one or more hydrocarbons from a hydrocarbon mixture. More specifically, the separation membrane includes a porous support for which acid content is not substantially detected by ammonia temperature programmed desorption in a temperature range of higher than 450° C. and not higher than 600° C. and a porous separation layer containing a zeolite that is disposed on the porous support.

A separation method includes a separation step of using a zeolite membrane composite to separate a branched diolefin from a branched hydrocarbon mixture containing the branched diolefin and at least one branched hydrocarbon in which the number of carbon-carbon double bonds is 1 or less and that is of an equivalent carbon number n to the branched diolefin. The zeolite membrane composite used in this step is a zeolite membrane composite that includes a porous support and a FAU-type zeolite membrane formed on at least one surface of the porous support, and in which the FAU-type zeolite membrane is a silylated FAU-type zeolite membrane including a silyl group at the surface thereof.

A separation method includes a separation step of using a zeolite membrane composite to separate a branched diolefin from a branched hydrocarbon mixture containing the branched diolefin and at least one branched hydrocarbon in which the number of carbon-carbon double bonds is 1 or less and that is of an equivalent carbon number n to the branched diolefin. The zeolite membrane composite used in this step is a zeolite membrane composite that includes a porous support and a FAU-type zeolite membrane formed on at least one surface of the porous support, and in which the FAU-type zeolite membrane is a silylated FAU-type zeolite membrane including a silyl group at the surface thereof.

A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. A naphtha feed stream may be separated into a normal paraffin stream and a non-normal paraffin stream. An isomerization feed stream may be taken from the non-normal paraffin stream and isomerized over an isomerization catalyst to convert non-normal paraffins to normal paraffins and produce an isomerization effluent stream. The isomerization effluent stream may be separated into a propane stream and a C4+ hydrocarbon stream optionally in a single column. The C4+ hydrocarbon stream may be recycled to the step of separating a naphtha feed stream.

A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. A naphtha feed stream may be separated into a normal paraffin stream and a non-normal paraffin stream. An isomerization feed stream may be taken from the non-normal paraffin stream and isomerized over an isomerization catalyst to convert non-normal paraffins to normal paraffins and produce an isomerization effluent stream. The isomerization effluent stream may be separated into a propane stream and a C4+ hydrocarbon stream optionally in a single column. The C4+ hydrocarbon stream may be recycled to the step of separating a naphtha feed stream.

The present disclosure provides for a separations system for separating ethylene, 2-methylbutane and at least one unsubstituted (C6-C12) hydrocarbon in a multi-component condensate mixture. The separations system includes a feed conduit in fluid communication with a source of the multi-component condensate mixture, a stripper column in fluid communication with the feed conduit, where the stripper column separates the multi-component condensate mixture into a heavies component mixture with at least one unsubstituted (C6-C12) hydrocarbon, and a top mixture having a medium component (s) that include at least the 2-methylbutane and a light component (s) that include at least the ethylene. The separations system further includes a flash drum that separates the top mixture into the medium component (s) and the light component (s). The separations system does not include a distillation column disposed between the source of the multi-component condensate mixture and the flash drum.