Natural gas liquid fractionation plant waste heat conversion to simultaneous power and potable water using kalina cycle and modified multi-effect-distillation system

Patent metadata

Field	Value
Publication number	US-11078809-B2
Application number	US-201916685412-A
Country	US
Kind code	B2
Filing date	Nov 15, 2019
Priority date	Aug 8, 2017
Publication date	Aug 3, 2021
Grant date	Aug 3, 2021

Abstract

Flowing a first buffer fluid and a second buffer fluid through a heat exchanger network thermally coupled to heat sources of a Natural Gas Liquid (NGL) fractionation plant, and transferring heat from the heat sources to the first buffer fluid and the second buffer fluid. Generating power via a first sub-system thermally coupled to the heat exchanger network and generating potable water from brackish water via a second sub-system thermally coupled to the heat exchanger network.

First claim

The invention claimed is:

1. A method of recovering heat, comprising:
flowing a first buffer fluid through a heat exchanger in a Natural Gas Liquid (NGL) fractionation plant, wherein the NGL fractionation plant comprising a dehydrator column, a distillation column, and a compressor;
transferring heat, via the heat exchanger, from the NGL fractionation plant to the buffer fluid; and
generating power with heat from the buffer fluid in a Kalina cycle system comprising a power turbine.

2. The method of claim 1 , wherein the compressor comprises a de-ethanizer refrigeration compressor in a de-ethanizer section comprising a de-ethanizer distillation column of the NGL fractionation plant, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an outlet stream from the de-ethanizer refrigeration compressor.

3. The method of claim 1 , wherein the NGL fractionation plant comprises a propane dehydration section comprising the dehydrator column as a propane dehydrator column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid with heat carried by a propane de-hydration outlet stream from the propane de-hydration section.

4. The method of claim 1 , wherein the NGL fractionation plant comprises a de-propanizer section comprising the distillation column as a de-propanizer distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an overhead outlet stream from the de-propanizer distillation column.

5. The method of claim 1 , wherein the NGL fractionation plant comprises a de-pentanizer section comprising the distillation column as a de-pentanizer distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid with heat carried by an overhead outlet stream from the de-pentanizer distillation column.

6. The method of claim 1 , wherein a third subset of the compressor comprises a propane main compressor in a propane product sub-cooling section in the NGL fractionation plant, wherein transferring heat via the heat exchanger comprises heating the buffer fluid with heat carried by an outlet stream from the propane main compressor, and wherein the propane product sub-cooling section further comprises a propane condenser heat exchanger.

7. The method of claim 1 , wherein the NGL fractionation plant comprises a butane de-hydrator section comprising the dehydrator column as a butane dehydrator column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an outlet stream of the butane dehydrator column.

8. The method of claim 1 , wherein the NGL fractionation plant comprises a de-butanizer section comprising the distillation column as a de-butanizer distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an overhead outlet stream from the de-butanizer distillation column or with heat carried by a bottoms outlet stream from the de-butanizer distillation column.

9. The method of claim 1 , comprising:
flowing the buffer fluid from a storage tank to the heat exchanger;
flowing the buffer fluid from the heat exchanger via a collection header conduit to the Kalina cycle system; and
flowing the buffer fluid from the Kalina cycle system to the storage tank.

10. The method of claim 1 , wherein the NGL fractionation plant comprises an Amine-Di-Iso-Propanol (ADIP) regeneration section comprising the distillation column as an ADIP regeneration distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid with heat carried by an overhead outlet stream from the ADIP regeneration distillation column or with heat carried by a bottoms stream from the ADIP regeneration distillation column.

11. The method of claim 1 , wherein the NGL fractionation plant comprises a natural gas de-colorizing section comprising the distillation column as a natural gas de-colorizer distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an overhead stream from the natural gas de-colorizer distillation column.

12. The method of claim 1 , wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an outlet stream discharged from the compressor, wherein the compressor is a propane refrigeration compressor in a propane product refrigeration section in the NGL fractionation plant, or wherein the compressor is a butane refrigeration compressor in a butane product refrigeration section in the NGL fractionation plant.

13. The method of claim 1 , wherein the NGL fractionation plant comprises a Reid Vapor Pressure (RVP) control section comprising the distillation column as a RVP distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid comprises with heat carried by an overhead outlet stream from the RVP distillation column.

14. The method of claim 1 , wherein the NGL fractionation plant comprises a natural gas de-colorizing section comprising the distillation column as a natural gas de-colorizer distillation column, and wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an overhead outlet stream from a pre-flash drum in the natural gas de-colorizing section.

15. A method of recovering heat, comprising:
flowing a buffer fluid through a heat exchanger in a Natural Gas Liquid (NGL) fractionation plant, the NGL fractionation plant comprising a distillation column and a compressor;
transferring heat, via the heat exchanger, from the NGL fractionation plant to the buffer fluid; and
generating power via a Kalina cycle system comprising a power turbine with heat from the buffer fluid.

16. The method of claim 15 , comprising:
flowing the buffer fluid from a storage tank to the heat exchanger;
flowing the buffer fluid from the heat exchanger via a collection header conduit to the Kalina cycle system; and
flowing the buffer fluid from the Kalina cycle system to the storage tank, wherein the buffer fluid comprises oil.

17. The method of claim 15 , wherein the Kalina cycle system partially vaporizes a mixture of ammonia and water with the heat from the buffer fluid to generate the power.

18. The method of claim 15 , wherein transferring heat via the heat exchanger comprises heating the buffer fluid in the heat exchanger with heat carried by an outlet stream discharged from the compressor, wherein the compressor is a propane vapor recovery compressor in a propane vapor recovery section in the NGL fractionation plant, the propane vapor recovery section further comprising a propane condenser heat-exchanger.

19. A method of recovering heat, comprising:
flowing a buffer fluid comprising oil through a heat exchanger in a Natural Gas Liquid (NGL) fractionation plant, wherein the NGL fractionation plant comprises a distillation column and a dryer vessel;
transferring heat, via the heat exchanger, from the NGL fractionation plant to the buffer fluid; and
generating power via a Kalina cycle system comprising a power turbine.

20. The method of claim 19 , wherein the NGL fractionation plant comprises an ethane production section comprising the dryer vessel as

Assignees

• Saudi Arabian Oil Co

Inventors

• Noureldin Mahmoud Bahy Mahmoud
• Kamel Akram Hamed Mohamed

Classifications

• Y02P70/10

  Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working · CPC title

• F25J2200/02

  in a single pressure main column system · CPC title

• F25J2215/62

  Ethane or ethylene · CPC title

• F25J3/0242

  separation of CnHm with 3 carbon atoms or more · CPC title

• F25J3/0209

  Natural gas or substitute natural gas · CPC title