Process of separating unsaturated hydrocarbons from saturated hydrocarbons with low energy consumption
Apparatuses, systems and methods for separating highly pure unsaturated olefinic hydrocarbon stream with zero cooling water and or steam consumption, with minimum possible capital investment and uncompromised operational ease are disclosed herein from a mixture of hydrocarbon stream consisting of saturated and unsaturated hydrocarbons. Embodiments of the invention are directed to producing a hydrocarbon stream containing polymer, chemical grade ethylene, propylene, butylenes, isoprene, hexane stream which are of value in manufacturing chemicals, polymers, and rubbers. Embodiments of the process provided can be applied to concentrating ethylene, propylene, butylenes, cyclopentadiene, isoprene, 2 methyl butene-2, isopentane, hexene etc.
1. A method for producing an unsaturated hydrocarbon stream, the method comprising:
providing a feed comprising saturated and unsaturated hydrocarbons to a hydrocarbon separation system, the hydrocarbon separation system comprising:
a low-pressure distillation column;
a high-pressure distillation column;
a compressor comprising a compressor inlet coupled to the low-pressure distillation column and a compressor outlet coupled to the high-pressure distillation column;
a feed inlet for receiving the feed coupled to one of the low-pressure distillation column and the high-pressure distillation column for receiving the feed; and
a closed-loop recirculating coolant system comprising:
a condenser coupled to the high-pressure distillation column; and
a reboiler coupled to the low-pressure distillation column with the coolant being circulated through the condenser coupled to the high-pressure distillation column;
compressing, via the compressor, an overhead product from the low-pressure distillation column;
feeding the compressed overhead product to the high-pressure distillation column;
feeding a bottoms product from the high-pressure distillation column to a heat exchanger to exchange heat between the bottoms product of the high-pressure distillation column and a coolant from an external coolant source passing through the heat exchanger;
feeding the heat-exchanged bottoms product from the heat exchanger to the low-pressure distillation column; and
producing an unsaturated hydrocarbon stream from the high-pressure distillation column;
wherein the high-pressure distillation column operates at a pressure range of 12 to 20 kg/cm 2 g and the low-pressure distillation column operates at a pressure range of 3 to 8 kg/cm 2 g.
2. The method of claim 1 , wherein the feed inlet is coupled to the low-pressure distillation column.
3. The method of claim 1 , wherein the feed inlet is coupled to the high-pressure distillation column.
4. The method of claim 1 , wherein the low-pressure and high-pressure distillation columns are operated at a pressure ratio of between 2-4, wherein the pressure ratio refers to the pressure of the high-pressure distillation column to the pressure of the low-pressure distillation column.
5. The method of claim 1 , wherein the high-pressure distillation column operates at a temperature range of 30 to 100° C.
6. The method of claim 1 , wherein the low-pressure distillation column operates at a temperature range of 4 to 45° C.
7. The method of claim 1 , wherein the hydrocarbon separation system is used in combination with a selective hydrogenation unit to saturate alkynes.
8. The method of claim 1 , further comprising:
removing, from the low-pressure distillation column, a bottoms product comprising saturated hydrocarbons; and
wherein the bottoms product removed from the low-pressure distillation column is at a pressure of between 3-8 kg/cm 2 g.
9. The method of claim 1 , further comprising:
removing, from the low-pressure distillation column, a bottoms product comprising saturated hydrocarbons; and
wherein the bottoms product removed from the low-pressure distillation column is at a temperature of 5-20° C.