Low cost thermal coupling in ethylene recovery

• US 5,675,054 A
• Filed: 07/17/1995
• Issued: 10/07/1997
• Est. Priority Date: 07/17/1995
• Status: Expired due to Term

• Current Assignee: David Manley
• Original Assignee: David Manley
• Inventors: Manley, David, Haddad, Hazem
• Primary Examiner(s): Caldarola, Glenn A.
• Assistant Examiner(s): BULLOCK, IN SUK C
• Application Number:
  US08/503,486
• Time in Patent Office: 813 Days
• Field of Search: 585/809, 208/102, 208/103, 208/104, 208/354, 208/355, 208/358, 62/630, 203/71, 203/74, 203/75, 203/81, 203/82, 203/84
• US Class Current: 585/809
• CPC Class Codes: B01D 3/146 Multiple effect distillation
• CPC Class Codes: C10G 70/041 by distillation
• CPC Class Codes: F25J 2200/38 using pre-separation or distributed distillation before a main column system, e.g. in a at least a double column system
• CPC Class Codes: F25J 2200/40 Features relating to the provision of boil-up in the bottom of a column
• CPC Class Codes: F25J 2200/80 using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
• CPC Class Codes: F25J 2210/12 Refinery or petrochemical off-gas
• CPC Class Codes: F25J 2215/62 Ethane or ethylene
• CPC Class Codes: F25J 2270/88 Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
• 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 3/0238 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0242 separation of CnHm with 3 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

Abstract

The invention is a process for reducing capital and energy costs in ethylene recovery. Moderate pressure processing and thermally coupled fractionation steps are achieved through the use of integrator columns. Ethylene separation from cracked gas originating from ethane through gas oil feeds can now be done with thermodynamically efficient fractionation at capital cost competitive with low efficiency designs. Acetylene hydrogenation may be done before demethanization where desired, and dephlegmation is preferred to accomplish high-efficiency rectification of hydrogen and methane from ethylene. Open loop heat pumps can optionally be incorporated into the ethane/ethylene splitter fractionation step, whose desirability is controlled by optimization of capital and energy costs.

Claims

1. A process for fractionation of a mixture of light hydrocarbons containing at least hydrogen, methane, ethylene, and ethane and optionally propylene and heavier hydrocarbons comprising:

(a) achieving a product-quality separation of at least a portion of the light hydrocarbons comprising hydrogen, methane, ethylene and ethane in a first integrator column to produce a first overhead stream and a first bottoms stream;

(b) fractionating the first overhead stream to produce a second bottoms stream comprising substantially a portion of a single component of one of said light hydrocarbons; and

(c) fractionating the first bottoms stream separately from the first overhead stream to produce a second overhead stream comprising substantially the remaining portion of the said single light hydrocarbon component in (b).

2. The process of claim 1 wherein the ethylene is the single light hydrocarbon.

3. The process of claim 2 wherein the first overhead stream is fractionated in a demethanizer, the first bottom stream is fractionated in a ethane/ethylene splitter, and the first integrator column is an ethylene integrator column.

4. The process of claim 3 wherein a demethanizer liquid sidestream provides reflux to the ethylene integrator column.

5. The process of claim 4 wherein an intercondenser is provided in the demethanizer.

6. The process of claim 5 wherein ethylene is recovered from a hydrogen-rich stream by dephlegmation in association with the demethanizer.

7. The process of claim 4 wherein a first portion of the overhead vapor from the ethane/ethylene splitter is fed to the bottom of the demethanizer as reboiling vapor and a second portion is withdrawn as ethylene product.

8. The process of claim 6 wherein a sidedraw vapor stream from the ethane/ethylene splitter is fed to the bottom of the ethylene integrator column as reboiling vapor.

9. The process of claim 6 wherein the ethane/ethylene splitter is provided with an interreboiler.

10. The process of claim 8 wherein the interreboiler is an open loop heat pumped refrigeration system partitioning the ethane/ethylene splitter into an upper high pressure section and a reduced pressure lower section.

11. The process of claim 3 wherein the mixture of light hydrocarbons is first fractionated in a deethanizer whose overhead stream is fed to the ethylene integrator column.

12. The process of claim 11 wherein the reflux to the deethanizer is provided entirely or in part from a side draw liquid stream from the ethylene integrator column.

13. The process of claim 3 wherein:

(a) the mixture of light hydrocarbons is first fractionated in an ethane/ethylene integrator column whose overhead vapor stream is substantially free of C3+ components and comprises a substantial portion but less than all of the ethane and ethylene in the mixture of light hydrocarbons;

(c) feeding the overhead vapor stream of the ethane/ethylene integrator column to the ethylene integration column;

(d) fractionating the liquid bottoms stream of the ethane/ethylene integrator column in a deethanizer, whose overhead vapor stream is fractionated in the ethane/ethylene splitter; and

(e) fractionating the liquid bottoms stream of the ethane/ethylene integrator column in the ethane/ethylene splitter.

14. The process of claim 13 wherein the mixture of light hydrocarbons is cracked gas from ethane and a substantial amount of propane.

15. The process of claim 3 wherein:

(a) the mixture of light hydrocarbons is first fractionated in a propane/propylene integrator column whose overhead vapor stream is substantially free of C4+components and comprises a substantial portion but less than all of the propane and propylene in the mixture of light hydrocarbons;

(b) fractionating the overhead vapor stream of the propane/propylene integrator column in an ethane/ethylene integrator column whose overhead vapor stream is substantially free of the C3+ components and comprises a substantial portion but less than all of the ethane and ethylene in the mixture of light hydrocarbons;

(c) feeding the overhead vapor stream of the ethane/ethylene integrator column to the ethylene integration column;

(d) fractionating the liquid bottoms stream of the ethane/ethylene integrator column and optionally part of the liquid bottoms stream of the ethylene integrator column in a deethanizer, whose overhead vapor stream is fed to the ethylene integrator column; and

(e) fractionating all or part of the liquid bottoms stream of the ethane/ethylene integrator column in the ethane/ethylene splitter.

16. The process of claim 15 wherein the mixture of light hydrocarbons is cracked gas from naphtha.

17. The process of claim 1 wherein:

(a) the mixture of light hydrocarbons is first fractionated in a C3/C4+ integrator column whose overhead vapor stream is substantially free of C5+ components and comprises a substantial portion but less than all of the C4 components in the mixture of light hydrocarbons;

(b) the mixture of light hydrocarbons is fractionated in a propane/propylene integrator column whose overhead vapor stream is substantially free of C4+ components and comprises a substantial portion but less than all of the propane and propylene in the mixture of light hydrocarbons;

(c) fractionating the overhead vapor stream of the propane/propylene integrator column in an ethane/ethylene integrator column whose overhead vapor stream is substantially free of the C3+ components and comprises a substantial portion but less than all of the ethane and ethylene in the mixture of light hydrocarbons;

(d) feeding the overhead vapor stream of the ethane/ethylene integrator column to the ethylene integration column;

(e) fractionating the liquid bottoms stream of the ethane/ethylene integrator column and optionally part of the liquid bottoms stream of the ethylene integrator column in a deethanizer, whose overhead vapor stream is fed to the ethylene integrator column to provide reboiling duty; and

(f) fractionating all or part of the liquid bottoms stream of the ethane/ethylene integrator column in the ethane/ethylene splitter.

18. The process of claim 17 wherein the mixture of light hydrocarbons is cracked gas from gas oil.

19. The process of claims 13, 15, or 17 wherein the reboiling duty of the ethylene integrator column is at least in part supplied by a side drawn vapor from the ethane/ethylene splitter and optionally in part supplied from the overhead vapor stream of the deethanizer.

20. The process of claim 1 wherein a net ethylene product is substantially obtained only from the overhead vapor of the ethane/ethylene splitter and reflux to the ethane/ethylene splitter is obtained at least in part from a liquid bottom from the demethanizer.

21. The process of claims 13, 15, or 17 wherein the reflux duty of the deethanizer is supplied at least in part by a side drawn liquid from the ethane/ethylene splitter and optionally supplied in part by a bottoms liquid stream from the ethylene integrator column.