DIRECT EVAPORATOR APPARATUS AND ENERGY RECOVERY SYSTEM

• US 20110061388A1
• Filed: 09/15/2009
• Published: 03/17/2011
• Est. Priority Date: 09/15/2009
• Status: Abandoned Application

• Current Assignee: General Electric Company
• Original Assignee: General Electric Company
• Inventors: Aumann, Richard, Lehar, Matthew Alexander, Ast, Gabor, Freund, Sebastian W., Frey, Thomas Johannes
• Application Number:
  US12/559,871
• Publication Number:
  US 20110061388A1
• Time in Patent Office: Days
• US Class Current: 60/653
• CPC Class Codes: F01K 23/10 with exhaust fluid of one cycle heating the fluid in another cycle F01K17/025 takes precedence
• CPC Class Codes: F01K 25/10 the vapours being cold, e.g. ammonia, carbon dioxide, ether
• CPC Class Codes: F01N 5/02 the devices using heat
• CPC Class Codes: F22B 1/1807 using the exhaust gases of combustion engines
• CPC Class Codes: F28D 21/001 for thermal power plants or industrial processes
• CPC Class Codes: F28D 7/1623 with particular pattern of flow of the heat exchange media, e.g. change of flow direction
• CPC Class Codes: Y02E 20/30 Technologies for a more efficient combustion or heat usage
• CPC Class Codes: Y02T 10/12 Improving ICE efficiencies

Abstract

In one aspect of the present invention provides a direct evaporator apparatus for use in an organic Rankine cycle energy recovery system, comprising: (a) a housing comprising a heat source gas inlet, and a heat source gas outlet, said housing defining a heat source gas flow path from said inlet to said outlet; and (b) a heat exchange tube disposed entirely within said heat source flow path, said heat exchange tube being configured to accommodate an organic Rankine cycle working fluid, said heat exchange tube comprising a working fluid inlet and a working fluid outlet, said heat exchange tube defining three zones, a first zone adjacent to said heat source gas outlet, a second zone adjacent to said heat source gas inlet, and a third zone disposed between said first zone and said second zone, said working fluid inlet being in direct fluid communication with said first zone, and said working fluid outlet being in direct fluid communication with said third zone; wherein said first zone is not in direct fluid communication with said third zone. An organic Rankine cycle energy recovery system and a method of energy recovery are also provided.

Claims

1. A direct evaporator apparatus for use in an organic Rankine cycle energy recovery system, comprising:

(a) a housing comprising a heat source gas inlet, and a heat source gas outlet, said housing defining a heat source gas flow path from said inlet to said outlet; and

(b) a heat exchange tube disposed entirely within said heat source flow path, said heat exchange tube being configured to accommodate an organic Rankine cycle working fluid, said heat exchange tube comprising a working fluid inlet and a working fluid outlet, said heat exchange tube defining three zones, a first zone adjacent to said heat source gas outlet, a second zone adjacent to said heat source gas inlet, and a third zone disposed between said first zone and said second zone, said working fluid inlet being in direct fluid communication with said first zone, and said working fluid outlet being in direct fluid communication with said third zone;

wherein said first zone is not in direct fluid communication with said third zone.

2. The direct evaporator apparatus according to claim 1, wherein said heat exchange tube comprises a plurality of bends in each of the first zone, second zone and third zone.

3. The direct evaporator apparatus according to claim 2, wherein the heat exchange tube is configured in parallel rows in each of the first zone, second zone and third zone.

4. The direct evaporator apparatus according to claim 3, wherein in each of the first zone, second zone and third zone of the heat exchange tube is configured in at least one row.

5. An organic Rankine cycle energy recovery system comprising:

(a) a direct evaporator apparatus comprising (i) a housing comprising a heat source gas inlet and a heat source gas outlet, said housing defining a heat source gas flow path from said inlet to said outlet; and

(ii) a heat exchange tube disposed entirely within said heat source flow path, said heat exchange tube being configured to accommodate an organic Rankine cycle working fluid, said heat exchange tube comprising a working fluid inlet and a working fluid outlet, said heat exchange tube defining three zones, a first zone adjacent to said heat source gas outlet, a second zone adjacent to said heat source gas inlet, and a third zone disposed between said first zone and said second zone, said working fluid inlet being in direct fluid communication with said first zone, and said working fluid outlet being in direct fluid communication with said third zone;

(b) work extraction device;

(c) a condenser; and

(d) a pump;

wherein the direct evaporator apparatus, work extraction device, condenser and pump a configured to operate as a closed loop.

6. The energy recovery system according to claim 5, wherein said heat exchange tube comprises a plurality of bends in each of the first zone, second zone and third zone.

7. The energy recovery system according to claim 5, wherein the heat exchange tube is configured in parallel rows in each of the first zone, second zone and third zone.

8. The energy recovery system according to claim 5, further comprising a recouperator.

9. The energy recovery system according to claim 5, wherein the work extraction device comprises a turbine.

10. The energy recovery system according to claim 9, further comprising a turbine by-pass duct.

11. A method of energy recovery comprising:

(a) introducing a heat source gas having a temperature into a direct evaporator apparatus containing a liquid working fluid;

(b) transferring heat from the heat source gas having a temperature T1 to the working fluid to produce a superheated gaseous working fluid and a heat source gas having temperature T2;

(c) expanding the superheated gaseous working fluid having a temperature T3 through a work extraction device to produce mechanical energy and a gaseous working fluid having a temperature T4;

(d) condensing the gaseous working fluid to provide a liquid state working fluid; and

(e) returning the liquid state working fluid to the direct evaporator apparatus;

wherein the direct evaporator apparatus comprises (i) a housing comprising a heat source gas inlet, and a heat source gas outlet, said housing defining a heat source gas flow path from said inlet to said outlet; and

a heat exchange tube disposed entirely within said heat source flow path, said heat exchange tube being configured to accommodate the working fluid, said heat exchange tube comprising a working fluid inlet and a working fluid outlet, said heat exchange tube defining three zones, a first zone adjacent to said heat source gas outlet, a second zone adjacent to said heat source gas inlet, and a third zone disposed between said first zone and said second zone, said working fluid inlet being in direct fluid communication with said first zone, and said working fluid outlet being in direct fluid communication with said third zone; and

wherein said first zone is not in direct fluid communication with said third zone.

12. The method according to claim 11, wherein the heat source gas has a temperature T1 in a range from about 400°

C. to about 600°

C.

13. The method according to claim 11, wherein the heat source gas has a temperature T2 in a range from about 100°

C. to about 250°

C.

14. The method according to claim 11, wherein the working fluid is a hydrocarbon.

15. The method according to claim 11, wherein the working fluid is a hydrocarbon is selected from the group consisting of methylcyclobutane, cyclopentane, isopentane, cyclohexane, and methycyclopentane.

16. The method according to claim 11, wherein the superheated gaseous working fluid has a temperature T3 in a range from below 300°

C.

17. The method according to claim 11, wherein the work extraction device is a turbine

18. The method according to claim 11, wherein the working fluid in the first zone is at a temperature in a range from about 20°

C. to about 150°

C.

19. The method according to claim 11, wherein the working fluid in the second zone is at a temperature in a range from about 50°

C. to about 300°

C.

20. The method according to claim 11, wherein the working fluid in the third zone is at a temperature in a range from about 200°

C. to about 300°

C.