Natural gas liquid fractionation plant waste heat conversion to power using Kalina cycle

Patent metadata

Field	Value
Publication number	US-10451359-B2
Application number	US-201715842515-A
Country	US
Kind code	B2
Filing date	Dec 14, 2017
Priority date	Aug 8, 2017
Publication date	Oct 22, 2019
Grant date	Oct 22, 2019

Abstract

Certain aspects of natural gas liquid fractionation plant waste heat conversion to power using Kalina Cycle can be implemented as a system. The system includes a waste heat recovery heat exchanger configured to heat a buffer fluid stream by exchange with a heat source in a natural gas liquid fractionation plant. The system includes a Kalina cycle energy conversion system, which includes one or more first energy conversion heat exchangers configured to heat a working fluid by exchange with the heated buffer fluid stream, a separator configured to receive the heated working fluid and to output a vapor stream of the working fluid and the liquid stream of the working fluid, and a turbine and a generator, wherein the turbine and generator are configured to generate power by expansion of the vapor stream of the working fluid.

First claim

The invention claimed is:

1. A system comprising:
a waste heat recovery heat exchanger configured to heat a buffer fluid stream by exchange with a heat source in a natural gas liquid fractionation plant;
a Kalina cycle energy conversion system including:
one or more first energy conversion heat exchangers configured to heat a working fluid by exchange with the heated buffer fluid stream;
a separator configured to receive the heated working fluid and to output a vapor stream of the working fluid and the liquid stream of the working fluid; and
a turbine and a generator, wherein the turbine and generator are configured to generate power by expansion of the vapor stream of the working fluid.

2. The system of claim 1 , wherein the turbine and generator are configured to generate at least 40 MW of power.

3. The system of claim 1 , wherein the energy conversion system comprises a pump configured to pump the working fluid to a pressure of between 7 Bar and 8 Bar.

4. The system of claim 1 , wherein the one or more first energy conversion heat exchangers comprise:
an energy conversion heat exchanger having a thermal duty of between 250 MM Btu/h and 350 MM Btu/h; and
an energy conversion heat exchanger having a thermal duty of between 1300 MM Btu/h and about 1500 MM Btu/h.

5. The system of claim 1 , wherein the one or more first energy conversion heat exchangers are configured to heat a first portion of the working fluid, and wherein the Kalina cycle energy conversion system comprises one or more second energy conversion heat exchangers configured to heat a second portion of the working fluid by exchange with the liquid stream of the working fluid.

6. The system of claim 5 , wherein the separator is configured to receive the heated first and second portions of the working fluid.

7. The system of claim 5 , wherein the one or more second energy conversion heat exchangers are configured to heat the second portion of the working fluid by exchange with the heated buffer fluid stream.

8. The system of claim 1 , comprising a second turbine configured to generate power from the liquid stream of the working fluid.

9. The system of claim 8 , wherein the second turbine is configured to generate at least 1 MW of power.

10. The system of claim 8 , wherein the second turbine comprises a high pressure recovery turbine.

11. The system of claim 1 , wherein the Kalina cycle energy conversion system comprises a cooler configured to cool the vapor stream of the working fluid and the liquid stream of the working fluid after power generation, wherein the cooler has a thermal duty of between 2500 MM Btu/h and 3500 MM Btu/h.

12. The system of claim 1 , comprising a storage tank, wherein the buffer fluid stream flows from the storage tank, through the waste heat recovery heat exchanger, through the Kalina cycle energy conversion system, and back to the storage tank.

13. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with a refrigerant in the natural gas liquid fractionation plant.

14. The system of claim 13 , wherein the refrigerant is used to cool ethane gas output from a deethanizer in the natural gas liquid fractionation plant.

15. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with propane gas output from a depropanizer in the natural gas liquid fractionation plant.

16. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with propane gas output from a propane dehydrator in the natural gas liquid fractionation plant.

17. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with a C5+ bottoms product from a debutanizer in the natural gas liquid fractionation plant.

18. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a debutanizer in the natural gas liquid fractionation plant.

19. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with butane gas output from a butane dehydrator in the natural gas liquid fractionation plant.

20. The system of claim 1 , wherein the waste heat recovery heat exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from a depentanizer in the natural gas liquid fractionation plant.

21. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with acid gases output from an ADIP generator in the natural gas liquid fractionation plant.

22. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with lean ADIP output from an ADIP generator in the natural gas liquid fractionation plant.

23. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with light NG components output from a pre-flash drum in a decolorizing section of the natural gas liquid fractionation plant.

24. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with NG gas output from a decolorizer in the natural gas liquid fractionation plant.

25. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with compressed propane in the natural gas liquid fractionation plant.

26. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with compressed butane in the natural gas liquid fractionation plant.

27. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with dry ethane gas in the natural gas liquid fractionation plant.

28. The system of claim 1 , wherein the waste heat recovery exchanger is configured to heat the buffer fluid stream by exchange with pentane gas output from an RVP column in the natural gas liquid fractionation plant.

29. A method comprising:
heating a buffer fluid stream via a waste heat recovery heat exchanger by exchange with a heat source in a natural gas liquid fractionation plant; and
generating power in a Kalina cycle energy conversion system, comprising:
heating a working fluid via one or more first energy conversion heat exchangers by exchange with the heated buffer fluid stream;

separating, in a separator, the heated working fluid into a vapor stream of the working fluid and the liquid stream of the working fluid; and
generating power, by a first turbine and generator, by expansion of the vapor stream of the working fluid.

30. The method of claim 29 , wherein generating power by the first turbine and generator includes generating at least 40 MW of power.

31. The method of claim 29 , comprising pumping the working fluid to a pressure of between 7 Bar and 8 Bar.

32. The method of claim 29 , wherein heating the working fluid comprises heating the working fluid to a temperature of between 160

Assignees

• Saudi Arabian Oil Co

Inventors

• Noureldin Mahmoud Bahy Mahmoud
• Kamel Akram Hamed Mohamed

Classifications

• F25J3/0242

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

• F01K25/10

  the vapours being cold, e.g. ammonia, carbon dioxide, ether · CPC title

• B01D3/146

  Multiple effect distillation · CPC title

• B01D3/065

  Multiple-effect flash distillation (more than two traps) · CPC title

• C10G7/00

  Distillation of hydrocarbon oils · CPC title