Ethane recovery methods and configurations
Contemplated methods and configurations use a cooled ethane and CO2-containing feed gas that is expanded in a first turbo-expander and subsequently heat-exchanged to allow for relatively high expander inlet temperatures to a second turbo expander. Consequently, the relatively warm demethanizer feed from the second expander effectively removes CO2 from the ethane product and prevents carbon dioxide freezing in the demethanizer, while another portion of the heat-exchanged and expanded feed gas is further chilled and reduced in pressure to form a lean reflux for high ethane recovery.
1. A gas processing plant for processing a feed gas, comprising:
a feed gas source configured to provide a feed gas comprising at least 0.5 mol % CO2 and less than 3 mol % C3+ components;
a first heat exchanger, a first turboexpander, and a second heat exchanger, coupled to each other in series upstream of a demethanizer and configured to cool and expand the feed gas to a pressure above a demethanizer operating pressure;
a separator fluidly coupled to the second heat exchanger and configured to separate the cooled and expanded feed gas into a liquid phase and a vapor phase;
a second turboexpander coupled to the separator and configured to expand a first portion of the vapor phase to the demethanizer pressure, and to deliver the expanded first portion to a top section of the demethanizer;
wherein the first heat exchanger, the first turboexpander, and the second heat exchanger are configured such that the first portion of the vapor phase has a temperature suitable for stripping of CO2 from an ethane product in the demethanizer;
a third heat exchanger and a pressure reduction device that are coupled to each other and configured to receive and condense a second portion of the vapor phase to thereby form a reflux to the demethanizer;
a deethanizer configured to receive a bottom product of the demethanizer and a portion of a totally condensed deethanizer product as a reflux, and produce a deethanizer overhead product;
a fourth heat exchanger configured to use the deethanizer overhead product or a demethanizer overhead product as a heat source to heat a side draw of the demethanizer to a temperature suitable to strip CO2 from the ethane product in the demethanizer; and
a fifth heat exchanger configured to receive the deethanizer overhead product to provide cooling to the deethanizer overhead product, wherein the fourth heat exchanger or the fifth heat exchanger are configured to (i) receive the overhead deethanizer product and (ii) totally condense the deethanizer overhead product to thereby form the totally condensed deethanizer overhead product.
2. The plant of claim 1 wherein the first and second heat exchangers are thermally coupled to the demethanizer to provide at least part of a reboiling duty to the demethanizer.
3. The plant of claim 1 wherein the first turboexpander is mechanically coupled to a residue gas compressor.
4. The plant of claim 1 wherein the feed gas source is configured to provide feed gas at a pressure of at least 1500 psig.
5. The plant of claim 1 wherein the feed gas comprises at least 1.0 mol % CO2 and less than 3 mol % C3+ components.
6. The plant of claim 1 wherein the pressure above the demethanizer operating pressure is between 1000 psig and 1400 psig.
7. The plant of claim 1 wherein the first heat exchanger, the first turboexpander, and the second heat exchanger are configured to cool the feed gas so that the first portion of the vapor phase has a temperature of between 0° F. to 30° F.
8. The plant of claim 1 wherein the second turboexpander is configured such that the expanded first portion of the vapor phase has a temperature between −75° F. and −85° F. and a pressure between 400 psig and 550 psig.
9. The plant of claim 1 wherein the third heat exchanger and the pressure reduction device are configured to condense the another portion of the vapor phase at a temperature of equal or less than −130° F.
10. A method of separating ethane from an ethane-containing gas, comprising:
providing from a feed gas source a feed gas comprising at least 0.5 mol % CO2 and less than 3 mol % C3+ components;
cooling and expanding the feed gas upstream of a demethanizer from a feed gas pressure to a pressure above a demethanizer operating pressure;
separating a superheated vapor phase from the cooled and expanded feed gas and expanding a first portion of the superheated vapor phase in a turboexpander to the demethanizer operating pressure, and feeding the expanded first portion of the vapor phase to a top section of the demethanizer;
wherein the feed gas is cooled and expanded such that the first portion of the vapor phase has a temperature suitable for stripping of CO2 from an ethane product in the demethanizer;
cooling and expanding a second portion of the superheated vapor phase to generate a reflux, and feeding the reflux to the demethanizer;
heating a side draw of the demethanizer with a deethanizer overhead product or a demethanizer overhead product to a temperature suitable for stripping of CO2 from the ethane product in the demethanizer; and
cooling a deethanizer overhead product to generate a totally condensed deethanizer overhead product, and feeding a portion of the totally condensed overhead product to the deethanizer as a deethanizer reflux.
11. The method of claim 10 wherein the step of expanding the feed gas is performed in a further turboexpander that is optionally mechanically coupled to a compressor.
12. The method of claim 10 wherein the step of cooling the feed gas is performed using a heat exchanger that is configured to provide reboiling heat to the demethanizer.
13. The method of claim 10 wherein the feed gas has a pressure of at least 1500 psig.
14. The method of claim 10 wherein the feed gas comprises at least 1.0 mol % CO2 and less than 3 mol % C3+ components.
15. The method of claim 10 wherein the pressure above the demethanizer operating pressure is between 1000 psig and 1400 psig.
16. The method of claim 10 wherein the first portion of the vapor phase has a temperature of between 0° F. to 30° F.
17. The method of claim 10 wherein the expanded first portion of the vapor phase has a temperature between −75° F. and −85° F. and a pressure between 400 psig and 550 psig.
18. The method of claim 10 wherein the another portion of the superheated vapor phase is cooled such that the reflux has a temperature of equal or less than −130° F.