Apparatus and method for recovering light hydrocarbons from hydrogen containing gases

• US 4,496,381 A
• Filed: 02/01/1983
• Issued: 01/29/1985
• Est. Priority Date: 02/01/1983
• Status: Expired due to Fees

• Current Assignee: Stone & Webster Engineering Corporation
• Original Assignee: Stone & Webster Engineering Corporation
• Inventors: Norenburg, Johannes
• Primary Examiner(s): Sever, Frank
• Application Number:
  US06/462,982
• Time in Patent Office: 728 Days
• Field of Search: 62/24, 62/27, 62/28, 62/29, 62/30, 62/31, 62/32, 62/34, 62/38, 62/39, 62/42, 62/43, 62/44, 62/40, 208/347, 208/350, 208/351, 208/352, 208/354, 585/800
• US Class Current: 62/630
• CPC Class Codes: C07C 7/04 by distillation
• CPC Class Codes: F25J 2200/04 in a dual pressure main column system
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2205/02 using simple phase separation in a vessel or drum
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2210/12 Refinery or petrochemical off-gas
• CPC Class Codes: F25J 2245/02 Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2270/06 with multiple gas expansion loops
• CPC Class Codes: F25J 3/0219 Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
• CPC Class Codes: F25J 3/0233 separation of CnHm with 1 carbon atom or more
• CPC Class Codes: F25J 3/0238 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0252 separation of hydrogen production of hydrogen containing gas in general C01B3/00, e.g. separation of hydrogen or hydrogen containing gases form gaseous mixtures at low temperatures C01B3/506
• CPC Class Codes: Y10S 62/932 From natural gas

Abstract

A process and apparatus provide enhanced recovery of ethylene, hydrogen and methane from the effluent produced by cracking olefins. A cracked gas is fractionally condensed in several stages. The overhead vapor from the last stage is refluxed in a rectifier tower to enable recovery of residual light hydrocarbons such as ethylene in the cracked gas and for improving the purity and yield of hydrogen. The refrigeration for producing the reflux is obtained by expanding a portion of the overhead vapor from the rectifier tower. Preferably, the fractional condensates of the cracked gas and the ethylene rich bottoms product from the rectifier tower are directed to a demethanizer. The overhead vapor from the demethanizer can be directed to the rectifier tower for recovery of ethylene contained therein.

Claims

1. An apparatus comprising:

elements designed, dimensioned and arranged for recovering ethylene from a cracked gas containing ethylene, methane and hydrogen, said apparatus including,

(a) a rectifier tower through which the cracked gas passes;

(b) an overhead line extending from the rectifier tower;

(c) a refrigeration system in communication with the rectifier tower, said refrigeration system comprising;

indirection heat exchange means in communication with said rectifier tower for cooling and partially condensing an overhead vapor passing from said rectifier tower overhead line through the hot side of said indirect heat exchange means;

an expansion means in communication with said heat exchange means for expanding the non-condensed portion of the partially condensed overhead vapor discharged from the hot side of the heat exchange means and recirculating said non-condensed portion to the cold side of said indirect heat exchange means for refrigeration; and

(d) a reflux means in communication with the hot side of said indirect heat exchange means and said rectifier tower for directing the condensed portion of the partially condensed rectifier tower overhead vapor from the hot side of the heat exchange means to the rectifier tower for reflux, thereby producing an ethylene rich bottoms product from said rectifier tower.

2. An apparatus as in claim 1 further comprising a demethanizer in communication with said rectifier tower for recovering the ethylene from the ethylene rich bottoms product of said rectifier tower.

3. An apparatus as in claim 2 wherein said demethanizer tower includes an overhead line in communication with said rectifier tower for directing overhead vapor from said demethanizer to said rectifier tower, whereby the ethylene in the overhead vapor from the demethanizer is recovered in the rectifier tower.

4. An apparatus as in claim 1 wherein the source of the cracked gas is a pyrolysis unit for cracking ethane and further comprising a fractional condenser system between the pyrolysis unit and the rectifier tower, said fractional condenser system separating the cracked effluent from the pyrolysis unit into a liquid fraction and an ethylene containing overhead vapor product which is directed to said rectifer tower and a demethanizer into which said liquid fraction from the fractional condenser system is delivered for the recovery of ethylene.

5. An apparatus as in claim 4 further comprising means for providing communication between said demethanizer and said rectifier tower for delivery of the bottoms product from said rectifier tower to said demethanizer, and for delivery of the overhead product from said demethanizer to said rectifier tower for recovering the ethylene therein.

6. An apparatus as in claim 1 wherein the overhead vapor directed through said rectifier tower overhead line comprises hydrogen, methane and ethylene.

7. An apparatus as in claim 1 wherein said ethylene containing gas is a vapor fraction of cracked ethane.

8. A method for recovering ethylene from a cracked gas comprised of ethylene, methane and hydrogen comprising the steps of:

(a) directing a stream of the cracked gas to a rectifier tower;

(b) removing an overhead vapor from said rectifier tower;

(c) directing the overhead vapor from said rectifier tower through the hot side of an indirect heat exchanger;

(d) cooling and partially condensing said overhead vapor in the hot side of said heat exchanger;

(e) expanding and recirculating the non-condensed portion of the overhead vapor to the cold side of the indirect heat exchanger;

(f) refluxing the rectifier tower with the condensed portion of the overhead vapor; and

(g) recovering ethylene as a bottoms product from said rectifier tower.

9. A method as in claim 8, further comprising the steps of:

directing the bottoms product from the rectifier tower to a demethanizer;

processing the bottoms product from the rectifier tower in the demethanizer to produce an overhead vapor containing residual ethylene; and

directing the overhead vapor from the demethanizer to the rectifier tower to recover the residual ethylene therein.

10. A process as in claim 9 further comprising the steps of:

directing the ethylene rich liquid fraction from the fractional condenser system to a demethanizer; and

delivering the bottoms product from the rectifier to the demethanizer whereby over 99 percent of the ethylene is recovered in the demethanizer.

11. A method as in claim 8 wherein the ethylene containing gas is provided by

cracking ethane and further comprising the steps of

fractionally condensing the cracked ethane serially in several stages to provide a vapor fraction of ethylene containing gas and an ethylene rich liquid fraction, and delivering the vapor fraction to the rectifier tower.

12. A method as in claim 8 wherein the non-condensed portion of the overhead vapor from the rectifier tower comprises hydrogen and methane.

13. A method as in claim 8 further comprising the steps of:

(a) expanding and cooling the noncondensed portion of the rectifier tower overhead vapor from the hot side of the heat exchanger and

(c) circulating the expanded and cooled non-condensed portion of the rectifier tower overhead from the expansion turbine through the cold side of the heat exchanger.

14. A process as in claim 8 further comprising the step of:

separating the non-condensed portion of the overhead vapor from the hot side of the indirect heat exchanger into a methane stream and a stream of about 90 mole percent hydrogen, both the methane stream and 90 mole percent hydrogen stream being free of ethylene.

15. A process as in claim 14 further comprising the steps of:

passing the hydrogen stream through the cold side of the indirect heat exchanger;

passing the hydrogen stream issuing from the cold side of the indirect heat exchanger through an expansion turbine to cool the hydrogen stream; and

passing the expanded, cooled hydrogen stream through the cold side of the indirect heat exchanger.

16. A process as in claim 15 further comprising the steps of:

fractionally condensing the cracked gas serially in serveral stages to produce a vapor fraction of ethylene containing gas and an ethylene rich liquid fraction;

passing the methane stream through the cold side of the heat exchanger;

passing the hydrogen and methane streams discharging from the indirect heat exchanger in indirect heat exchange with the vapor fraction of ethylene containing gas from the fractional condensing step to further cool said vapor fraction; and

delivering the cooled vapor fraction to the rectifier tower.

17. A process as in claim 16 further comprising the steps of:

directing the ethylene rich liquid fraction from the fractional condenser system to a demethanizer; and

delivering the bottoms product from the rectifier to the demethanizer whereby over 99 percent of the ethylene is recovered in the demethanizer.

18. A process as in claim 17 wherein the overhead vapor fraction from the fractional condenser is at about -144°

F. when delivered to the rectifier tower;

the overhead from the demethanizer is at about -151°

F. when delivered to the rectifier tower;

the rectifier tower is operated at approximately 392 psia;

the overhead from the rectifier tower is approximately -203°

F.;

the reflux condensate is comprised of approximately 3 mole percent hydrogen;

97 mole percent methane and less than 0.1 percent ethylene;

the non-condensed overhead is 75 percent hydrogen and 25 percent methane and is further cooled to -245°

F. to produce a 90 mole percent hydrogen gas.