Efficient oxidative coupling of methane processes and systems
The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C 2+ compounds and non-C 2+ impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C 2+ impurities from the C 2+ compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react H 2 with CO and/or CO 2 in the non-C 2+ impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker.
1. A method for performing oxidative coupling of methane (OCM), the method comprising:
(a) providing a system comprising a substantially adiabatic OCM reactor, a cracking unit, a compressor, a separations unit, and a methanation reactor that are in fluid communication with one another;
(b) directing oxygen (O 2 ) and methane (CH 4 ) into said OCM reactor that reacts said O 2 and CH 4 in an OCM process to yield a product stream comprising (i) compounds with two or more carbon atoms (C 2+ compounds), including ethylene (C 2 H 4 ), and (ii) carbon monoxide (CO) or carbon dioxide (CO 2 ), wherein said OCM process liberates heat;
(c) directing said product stream comprising said C 2+ compounds and carbon monoxide (CO) or carbon dioxide (CO 2 ) from said OCM reactor and ethane from an ethane stream external to said OCM reactor directly into said cracking unit that cracks ethane (C 2 H 6 ) with the aid of energy derived from said heat liberated in said OCM process, thereby increasing a concentration of C 2 H 4 and hydrogen (H 2 ) in said product stream;
(d) directing said product stream from said cracking unit into said compressor, which compressor increases a pressure of said product stream with the aid of energy derived from said heat liberated in said OCM process;
(e) directing said product stream from said compressor into said separations unit, which separations unit enriches said C 2 H 4 in said product stream with the aid of energy derived from said heat liberated in said OCM process; and
(f) directing H 2 and CO or CO 2 from said product stream from said separations unit into said methanation reactor, which methanation reactor reacts said H 2 from said product stream with said CO or CO 2 from said product stream to form CH 4 ,
wherein a ratio of (i) all carbon atoms output from said system as hydrocarbons to (ii) all carbon atoms input to said system is at least about 0.50.
2. The method of claim 1 , wherein said carbon atoms output from said system as hydrocarbons include at least a portion of said C 2+ compounds and excludes CO and CO 2 .
3. The method of claim 1 , wherein said carbon atoms input to said system include said CH 4 directed into said OCM reactor in (b) and said ethane stream external to said OCM reactor directed into said cracking unit in (c).
4. The method of claim 1 , wherein at least a portion of said C 2 H 6 that is cracked in (b) is produced in said OCM reactor.
5. The method of claim 1 , wherein at least portion of said ethane stream is from said separations unit.
6. The method of claim 1 , wherein said product stream comprises CO and CO 2 , and wherein at least a portion of said CO and CO 2 from said product stream is methanated in (f).
7. The method of claim 1 , wherein said separations unit enriches said C 2+ compounds by removing CH 4 , H 2 , CO or CO 2 .
8. The method of claim 1 , wherein said cracking unit is integrated with said OCM reactor.
9. The method of claim 1 , wherein said cracking unit adiabatically cracks C 2 H 6 .
10. The method of claim 1 , wherein at least a portion of said CH 4 formed in (f) is returned to said OCM reactor.
11. The method of claim 1 , further comprising using a power generation unit in thermal communication with said OCM reactor to generate power from at least a portion of said heat liberated in said OCM process.
12. The method of claim 1 , wherein said product stream comprises C 2 H 6 and H 2 .
13. The method of claim 1 , wherein said methane in (b) and said ethane in (c) are derived from natural gas that is initially directed into said compressor or said separations unit.
14. The method of claim 1 , wherein said methanation reactor has a methanation catalyst that converts CO and/or CO 2 into CH 4 at a selectivity for the formation of CH 4 that is at least about 10-fold greater than a selectivity of said catalyst for formation of coke from said CO and/or CO 2 .
15. The method of claim 1 , wherein at least 90% of energy used to perform (b) through (f) is derived from said heat liberated in said OCM process.
16. The method of claim 1 , wherein said OCM reactor is a fixed bed OCM reactor.
17. The method of claim 1 , wherein said cracking unit is substantially adiabatic.
18. The method of claim 1 , wherein an inlet temperature of said OCM reactor is at most about 600° C.
19. The method of claim 1 , wherein at least 90% of energy used to perform (b) through (f) is derived from said heat liberated in said OCM process.