Organic flash cycles for efficient power production

Patent metadata

Field	Value
Publication number	US-9284857-B2
Application number	US-201313923159-A
Country	US
Kind code	B2
Filing date	Jun 20, 2013
Priority date	Jun 26, 2012
Publication date	Mar 15, 2016
Grant date	Mar 15, 2016

Abstract

This disclosure provides systems, methods, and apparatus related to an Organic Flash Cycle (OFC). In one aspect, a modified OFC system includes a pump, a heat exchanger, a flash evaporator, a high pressure turbine, a throttling valve, a mixer, a low pressure turbine, and a condenser. The heat exchanger is coupled to an outlet of the pump. The flash evaporator is coupled to an outlet of the heat exchanger. The high pressure turbine is coupled to a vapor outlet of the flash evaporator. The throttling valve is coupled to a liquid outlet of the flash evaporator. The mixer is coupled to an outlet of the throttling valve and to an outlet of the high pressure turbine. The low pressure turbine is coupled to an outlet of the mixer. The condenser is coupled to an outlet of the low pressure turbine and to an inlet of the pump.

First claim

We claim:

1. A system comprising:
a pump;
a heat exchanger, the heat exchanger coupled to an outlet of the pump, the heat exchanger operable to receive an organic fluid from the pump and to heat the organic fluid;
a flash evaporator, the flash evaporator coupled to an outlet of the heat exchanger, the flash evaporator operable to receive the heated organic fluid from the heat exchanger, the flash evaporator operable to flash evaporate the heated organic fluid to generate a high pressure organic vapor and an organic liquid;
a high pressure turbine, the high pressure turbine coupled to a vapor outlet of the flash evaporator, the high pressure turbine operable to be driven with the high pressure organic vapor received from the flash evaporator and to generate an intermediate pressure organic vapor;
a throttling valve, the throttling valve coupled to a liquid outlet of the flash evaporator, the throttling valve operable to reduce a pressure of the organic liquid received from the flash evaporator;
a mixer, the mixer coupled to an outlet of the throttling valve and to an outlet of the high pressure turbine, the mixer operable to mix the intermediate pressure organic vapor received from the high pressure turbine and the reduced pressure organic liquid received from the throttling valve to form a low pressure organic vapor;
a low pressure turbine, the low pressure turbine coupled to an outlet of the mixer, the low pressure turbine operable to be driven with the low pressure organic vapor received from the mixer and to reduce a pressure of the low pressure organic vapor; and
a condenser, the condenser coupled to an outlet of the low pressure turbine and to an inlet of the pump, the condenser operable to receive the reduced pressure low pressure organic vapor from the low pressure turbine and to generate a liquid state of the organic fluid, the condenser operable to deliver the liquid state of the organic fluid to the pump.

2. The system of claim 1 , wherein the high pressure turbine and the low pressure turbine are coupled to a generator.

3. The system of claim 1 , wherein the flash evaporator includes a pressure vessel and a second throttling value.

4. The system of claim 1 , wherein the organic fluid is selected from a group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).

5. A method using the system of claim 1 , the method comprising:
(a) compressing the organic fluid with the pump;
(b) delivering the organic fluid to the heat exchanger and heating the organic fluid by passing the organic fluid through the heat exchanger;
(c) delivering the heated organic fluid to the flash evaporator and flash evaporating the heated organic fluid to generate the high pressure organic vapor and the organic liquid;
(d) driving the high pressure turbine with the high pressure organic vapor from the flash evaporator and lowering a pressure of the high pressure organic vapor to form the intermediate pressure organic vapor;
(e) reducing the pressure of the organic liquid from the flash evaporator by passing the organic liquid through the throttling valve;
(f) mixing the reduced pressure organic liquid from the throttling valve and the intermediate pressure organic vapor from the high pressure turbine in the mixer to form the low pressure organic vapor;
(g) driving the low pressure turbine with the low pressure organic vapor from the mixer and reducing the pressure of the low pressure organic vapor;
(h) condensing the reduced pressure low pressure organic vapor from the low pressure turbine to the liquid state of the organic fluid with the condenser; and
(i) delivering the liquid state of the organic fluid from the condenser to the pump.

6. The method of claim 5 , wherein the high pressure turbine and the low pressure turbine are coupled to a generator, and wherein operations (d) and (g) generate electricity.

7. The method of claim 5 , wherein a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C.

8. The method of claim 5 , wherein a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.

9. The method of claim 5 , wherein the organic fluid is in a subcooled liquid state after operation (a).

10. The method of claim 5 , wherein the organic fluid is heated isobarically in operation (b).

11. The method of claim 5 , wherein the organic fluid remains in a liquid state in operation (b).

12. The method of claim 5 , wherein the heated organic fluid generated in operation (b) is in a saturated liquid state.

13. The method of claim 5 , wherein the intermediate pressure organic vapor generated in operation (d) comprises a saturated vapor or a superheated vapor.

14. The method of claim 5 , wherein the reduced pressure organic liquid generated in operation (e) comprises a liquid and vapor mixture.

15. The method of claim 5 , wherein the reduced pressure low pressure organic vapor generated in operation (g) comprises a saturated vapor or a superheated vapor.

16. A method comprising:
(a) compressing an organic fluid with a pump;
(b) delivering the organic fluid from the pump to a heat exchanger and heating the organic fluid by passing the organic fluid through the heat exchanger;
(c) delivering the organic fluid from the heat exchanger to a flash evaporator and flash evaporating the organic fluid to generate a high pressure organic vapor and an organic liquid;
(d) driving a high pressure turbine with the high pressure organic vapor from the flash evaporator and lowering a pressure of the high pressure organic vapor to form an intermediate pressure organic vapor;
(e) reducing a pressure of the organic liquid from the flash evaporator by passing the organic liquid through a throttling valve;
(f) mixing the reduced pressure organic liquid from the throttling valve and the intermediate pressure organic vapor from the high pressure turbine in a mixer to form a low pressure organic vapor;
(g) driving a low pressure turbine with the low pressure organic vapor from the mixer and reducing a pressure of the low pressure organic vapor;
(h) condensing the reduced pressure low pressure organic vapor from the low pressure turbine to a liquid state of the organic fluid with a condenser; and
(i) delivering the liquid state of the organic fluid from the condenser to the pump.

17. The method of claim 16 , wherein the high pressure turbine and the low pressure turbine are coupled to a generator, and wherein operations (d) and (g) generate electricity.

18. The method of claim 16 , wherein the organic fluid is selected from a group consisting of toluene, ethylbenzene, butylbenzene, o-xylene, m-xylene, p-xylene, tetradecamethylhexasiloxane (MD4M), tetradecamethylhexasiloxane (MD4M), decamethylcyclopentasiloxane (D5), dodecamethylpentasiloxane (MD3M), and dodecamethylcyclohexasiloxane (D6).

19. The method of claim 16 , wherein a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is about 80° C. to 400° C.

20. The method of claim 16 , wherein a temperature of a liquid or a vapor used to heat the organic fluid in the heat exchanger is below about 300° C.

Assignees

• Univ California

Inventors

• Ho Tony
• Mao Samuel S
• Greif Ralph

Classifications

• F01K25/10

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

• F22B3/04

  by drop in pressure of high-pressure hot water within pressure-reducing chambers, e.g. in accumulators · CPC title

• F01K25/08 Primary

  using special vapours · CPC title

• F01K13/02

  Controlling, e.g. stopping or starting · CPC title

• F01K23/10

  with exhaust fluid of one cycle heating the fluid in another cycle (F01K17/025 takes precedence) · CPC title