Systems and processes for heavy hydrocarbon removal
Disclosed herein are processes and systems for removing heavy C5+ hydrocarbon components from a natural gas feed gas by subjecting the natural gas feed gas stream to an adsorber. The adsorber in the processes and systems described herein operating at a pressure that may be associated with improved adsorption capacity and longer breakthrough time.
1. A method of removing C5+ hydrocarbons from a natural gas feed gas (FG) stream and sending to a natural gas liquids (NGL) recovery or liquefied natural gas (LNG) facility or a CO 2 removal processing unit and/or a pipeline, the method comprising:
routing the FG at a pressure P adsorber over an adsorber to adsorb C5+ hydrocarbon and provide a heavy hydrocarbon depleted natural gas (HHCDNG) stream at pressure P adsorber ranging from about 300 psia to about 1200 psia, wherein the adsorber comprises a hydrocarbon-selective adsorbent; and
routing the HHCDNG stream through one or more compressors to provide a HHCDNG at pressure P3, wherein P3>P adsorber , and wherein the adsorbent is configured to operate at the pressure P adsorber associated with increased adsorption capacity and/or longer breakthrough time of the C5+ hydrocarbons.
2. A method of removing C5+ hydrocarbons from a natural gas feed gas (FG) stream and sending to a natural gas liquids (NGL) recovery or liquefied natural gas (LNG) facility or a CO 2 removal processing unit or a pipeline, the method comprising:
routing the FG at a pressure P1 through one or more compressors to provide a FG stream at a pressure P adsorber ;
routing the FG stream at pressure P adsorber through an adsorber, to adsorb C5+ hydrocarbon and provide a heavy hydrocarbon depleted natural gas (HHCDNG) stream at pressure P adsorber , the adsorber comprising a hydrocarbon-selective adsorbent; and
routing the HHCDNG stream through one or more compressors to provide a HHCDNG at pressure P3, wherein P3>P1 and/or P3>P adsorber and/or P adsorber >P1, wherein P adsorber ranges from about 300 psia to about 1200 psia, and wherein the adsorbent is configured to operate at the pressure P adsorber associated with increased adsorption capacity and/or longer breakthrough time of the C5+ hydrocarbons.
3. The method of claim 2 , wherein P3 ranges from about 600 psi to about 2000 psia, from about 800 psia to about 1800 psia, or from about 1000 psia to about 1600 psia.
4. The method of claim 2 , wherein the adsorber is one or more of a pressure swing adsorber (PSA) or a thermal swing adsorber (TSA).
5. The method of claim 2 , wherein the adsorber is a thermal swing adsorber (TSA).
6. The method of claim 2 , wherein P adsorber ranges from about 350 psia to about 1050 psia, from about 400 psia to about 900 psia, from about 300 psia to about 700 psia, from about 350 psia to about 650 psia, or from about 400 psia to about 600 psia.
7. The method of claim 2 , wherein the FG stream is about 90% water saturated or less.
8. The method of claim 2 , wherein the FG stream comprises less than about 5%, less than about 4%, less than about 3%, less than about 2%, or less than about 1% carbon dioxide, on a molar basis based on the FG stream.
9. The method of claim 2 , wherein the HHCDNG comprises less than about 98%, less than about 95%, less than about 90%, less than about 80%, less than about 70%, less than about 60%, less than about 50%, less than about 40%, less than about 30%, less than about 20%, less than about 10%, less than about 8%, less than about 5%, less than about 3%, less than about 2%, or less than about 1%, C5+ components, calculated on a molar basis based on the HHCDNG stream.
10. The method of claim 2 , wherein the hydrocarbon-selective adsorbent has an internal BET surface area from about 100 m 2 /g to about 2000 m 2 /g.
11. The method of claim 2 , wherein the hydrocarbon-selective adsorbent is one or more of silica, silica gel, alumina, silica-alumina, molecular sieves, zeolites, or sorbead.
12. A system for removing C5+ hydrocarbons, comprising an adsorber comprising a hydrocarbon-selective adsorbent, the system being configured to route a feed gas (FG) stream at a pressure P adsorber over the adsorber to adsorb C5+ hydrocarbon and provide a heavy hydrocarbon depleted natural gas (HHCDNG) stream at pressure P adsorber ranging from about 300 psia to about 1200 psia, the system further comprising one or more compressors positioned after the adsorber configured to receive HHCDNG at pressure P adsorber and compress the HHCDNG to pressure P3, wherein P3>P adsorber , and wherein the adsorbent is configured to operate at the pressure P adsorber associated with increased adsorption capacity and/or longer breakthrough time of the C5+ hydrocarbons.
13. The system of claim 12 , wherein P adsorber ranges from about 350 psia to about 1050 psia, from about 400 psia to about 900 psia, from about 300 psia to about 700 psia, from about 350 psia to about 650 psia or from about 400 psia to about 600 psia.
14. The system of claim 12 , wherein the adsorber is one or more of a pressure swing adsorber (PSA) or a thermal swing adsorber (TSA).
15. The system of claim 12 , further comprising one or more compressors positioned before the adsorber configured to compress the FG stream at a pressure P1 such that the pressure of the FG stream existing the one or more compressors positioned before the adsorber and entering the adsorber is P adsorber .
16. The system of claim 15 , wherein P3>P adsorber and wherein P3 ranges from about 600 psi to about 2000 psia, from about 800 psia to about 1800 psia, or from about 1000 psia to about 1600 psia.
17. The system of claim 12 , wherein the FG stream is about 90% water saturated or less.
18. The system of claim 12 , wherein the HHCDNG comprises less than about 98%, less than about 95%, less than about 90%, less than about 80%, less than about 70%, less than about 60%, less than about 50%, less than about 40%, less than about 30%, less than about 20%, less than about 10%, less than about 8%, less than about 5%, less than about 3%, less than about 2%, or less than about 1% C5+ components, calculated on a molar basis based on the HHCDNG stream.
19. The system of claim 12 , wherein the hydrocarbon-selective adsorbent has an internal BET surface area from about 100 m 2 /g to about 2000 m 2 /g, and wherein the hydrocarbon-selective adsorbent is one or more of silica, silica gel, alumina, silica-alumina, molecular sieves, zeolites, or sorbead.
20. The system of claim 12 , further comprising one or more of a natural gas liquids (NGL) recovery facility, a liquefied natural gas (LNG) facility, a CO 2 removal processing unit, a pipeline for transporting natural gas retrieved from underground storage, positioned after the adsorber.