CN111577414A - Supercritical CO coupling separation of LNG light hydrocarbon2Recompression brayton/kalina combined cycle power generation system - Google Patents
Supercritical CO coupling separation of LNG light hydrocarbon2Recompression brayton/kalina combined cycle power generation system Download PDFInfo
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Abstract
Supercritical CO coupling separation of LNG light hydrocarbon2The recompression Brayton/kalina combined cycle power generation system comprises an LNG light hydrocarbon separation system, a light-gathering solar heat collection circulation system and a supercritical CO2Then compressing the Brayton cycle system, the kalina cycle system and the natural gas direct expansion system; the LNG light hydrocarbon separation system is used for recovering C2+ light hydrocarbon resources; the light-gathering solar heat collection circulating system is used for photo-thermal conversion;supercritical CO2Then, the compressed Brayton cycle system, the kalina cycle system and the natural gas direct expansion system are used for coupling LNG cold energy and high-temperature solar energy for power generation; the invention utilizes solar energy to carry out supercritical CO in daytime2The Brayton cycle power generation is compressed, the waste heat discharged by the Brayton cycle power generation is stored, and heat is continuously provided for the kalina cycle at night, so that the system reaches a continuous power generation state, and the effective recovery of C2+ light hydrocarbon resources and the efficient complementary utilization of LNG cold energy and solar energy are realized; has the advantages of reasonable and compact structure, safe and flexible control, high efficiency, energy conservation, strong practicability and low cost.
Description
Technical Field
The invention relates to an LNG cold energy and solar energy complementary utilization system, in particular to an LNG light hydrocarbon separation coupling supercritical CO2And then compressing the Brayton/kalina combined cycle power generation system.
Background
LNG (liquefied natural gas) needs to be gasified to normal temperature and then supplied to users. The LNG can release about 830-860 kWh/kg of cold energy in the gasification process, and if the cold energy can be utilized, great economic benefits can be generated. The C2+ light hydrocarbon component rich in LNG is a very high quality chemical feedstock that can be used to produce many high value added petrochemicals. The LNG cold energy is used for separating light hydrocarbon components, the LNG can be efficiently utilized, and the utilization rate of the LNG cold energy is not high.
Supercritical CO2The recompression Brayton cycle has the advantages of compact structure, high thermal efficiency, safety, environmental protection and the like, and has good application prospect in the field of solar thermal power generation, but the technology is restricted by the nonuniformity of solar energy distributed along with time. In the kalina cycle using an ammonia water mixture as a working medium, the heat absorption evaporation process of the working medium is a temperature changing process, so that the heat release process of a heat source can be better matched with the heat absorption process curve of the mixed working medium, the irreversible loss in the heat release process is reduced to the maximum extent, and the heat energy utilization efficiency is improved.The LNG is used as a cold source of the kalina cycle, so that the power generation efficiency can be further improved, but the utilization rate of the LNG cold energy is not high. The natural gas direct expansion power generation technology has the advantages of simple process, low cost and the like, but can only utilize the pressure energy of LNG and has the defect of low utilization rate of cold energy.
In conclusion, LNG light hydrocarbon separation and supercritical CO2The recompression Brayton cycle power generation and the kalina cycle power generation are only single utilization of LNG cold energy, so that the problems that the LNG cold energy is not fully utilized, the cold temperature level is not matched with the LNG temperature and the like exist.
Disclosure of Invention
In order to solve the defects of the prior art, the invention aims to provide an LNG light hydrocarbon separation coupling supercritical CO2Then compresses the Brayton/kalina combined cycle power generation system to separate LNG light hydrocarbon and supercritical CO2The recompression Brayton cycle, the kalina cycle, the solar photo-thermal power generation technology and the natural gas direct expansion power generation technology are combined, so that the C2+ light hydrocarbon resource with high added value can be effectively recovered, the high-efficiency complementary utilization of LNG cold energy and solar energy is realized, the problem of uneven distribution of the solar energy along with time is solved, and the photo-thermal power generation cost is greatly reduced; meanwhile, LNG cold energy is utilized in a cascade mode, and the heat efficiency and the power generation efficiency of a power generation system are effectively improved; has the advantages of reasonable and compact structure, safe and flexible control, high efficiency, energy conservation, strong practicability and low cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
supercritical CO coupling separation of LNG light hydrocarbon2The recompression Brayton/kalina combined cycle power generation system comprises an LNG light hydrocarbon separation system, a light-gathering solar heat collection circulation system and a supercritical CO2Then compressing the Brayton cycle system, the kalina cycle system and the natural gas direct expansion system;
the LNG light hydrocarbon separation system comprises an LNG pump 1, a working medium outlet side of the LNG pump 1 is connected to an inlet side of a first tee joint device 2, an outlet side of the first tee joint device 2 is divided into two branches, wherein, one outlet side is connected with a feeding port I of the demethanizer 6, the other outlet side is connected with a cold flow inlet side of the first heat exchanger 3, a cold flow outlet side of the first heat exchanger 3 is connected with a cold flow inlet side of the second heat exchanger 4, a cold flow outlet side of the second heat exchanger 4 is connected with a feeding port of the flash tower 5, a kettle liquid port of the flash tower 5 is communicated with a feeding port II of the demethanizer 6, a bottom discharge port of the demethanizer 6 is communicated with an inlet side of the first throttle valve 7, an outlet side of the first throttle valve 7 is connected with a feeding port of the deethanizer 8, a top discharge port of the deethanizer 8 is connected with a hot flow inlet side of the second heat exchanger 4, and a top discharge port of the flash tower 5 and a top discharge port of the demethanizer 6 are respectively communicated with two inlet sides of the first mixer 9;
the concentrating solar heat collection circulating system comprises a heliostat 29, the heliostat 29 absorbs sunlight and transfers heat to a heat absorber 28, a working medium outlet side of the heat absorber 28 is communicated with a working medium inlet side of a pump 27, a working medium outlet side of the pump 27 is communicated with a heat flow inlet side of a fourth heat exchanger 26, and a heat flow outlet side of the fourth heat exchanger 26 is communicated with a working medium inlet side of the heat absorber 28;
the supercritical CO2The recompression Brayton cycle system comprises a main compressor 19, wherein the outlet side of the main compressor 19 is communicated with the cold flow inlet side of a low-temperature heat regenerator 22, the cold flow outlet side of the low-temperature heat regenerator 22 and the outlet side of a recompressor 20 are connected into the cold flow inlet side of a high-temperature heat regenerator 24 through a third mixer 23, the cold flow outlet side of the high-temperature heat regenerator 24 is communicated with the cold flow inlet side of a fourth heat exchanger 26, and the cold flow outlet side of the fourth heat exchanger 26 is communicated with the supercritical CO2The inlet side of the turboexpander 25 is connected to supercritical CO2The outlet side of the turboexpander 25 is communicated with the heat flow inlet side of the high-temperature regenerator 24, the heat flow outlet side of the high-temperature regenerator 24 is communicated with the heat flow inlet side of the low-temperature regenerator 22, the heat flow outlet side of the low-temperature regenerator 22 is communicated with the inlet side of the second tee joint 21, the outlet side of the second tee joint 21 is divided into two parts, one part is connected to the inlet side of the recompressor 20, the other part is connected to the heat flow inlet side of the precooler 15, and the heat flow outlet side of the precooler 15 is communicated with the inlet side of the main compressor 19;
the kalina circulation system comprises a first ammonia water pump 14, wherein a working medium outlet side of the first ammonia water pump 14 is connected with a cold flow inlet side of a precooler 15, a cold flow outlet side of the precooler 15 is connected with a working medium inlet side of a separator 16, a gas phase outlet end of the separator 16 is communicated with an air inlet of an ammonia gas turbine expander 17, an air outlet of the ammonia gas turbine expander 17 is communicated with a heat flow inlet side of a first heat exchanger 3, a heat flow outlet side of the first heat exchanger 3 is connected with a working medium inlet side of a second ammonia water pump 18, a liquid phase outlet end of the separator 16 is communicated with a heat flow inlet side of a third heat exchanger 10, a heat flow outlet side of the third heat exchanger 10 is connected with an inlet side of a second throttle valve 12, and a working medium outlet side of the second ammonia water pump 18 and an outlet side of the second throttle valve 12 are connected with the working medium inlet side of the first ammonia;
the natural gas direct expansion system comprises a first mixer 9, wherein the outlet side of the first mixer 9 is communicated with the cold flow inlet side of a third heat exchanger 10, and the cold flow outlet side of the third heat exchanger 10 is communicated with the inlet side of a turbine expander 11.
The working medium at the working medium inlet side of the LNG pump 1 is liquefied natural gas.
The working medium at the bottom discharge hole of the deethanizer 8 is liquefied petroleum gas.
And the working medium on the heat flow outlet side of the second heat exchanger 4 is liquid ethane.
The supercritical CO2Recompression of the circulating medium in the Brayton cycle as supercritical CO2。
And the circulating medium in the kalina cycle is an ammonia water mixture.
The outlet side of the turboexpander 11 is directly connected to a user or a company.
The invention has the beneficial effects that:
c2+ light hydrocarbon resources in the LNG are recovered through a light hydrocarbon separation process flow, and partial cold energy of the LNG is utilized; LNG and methane-rich natural gas separated from light hydrocarbon are used as a cold source of kalina circulation, and the cooled ammonia water mixture is used as supercritical CO2Then the cold source of Brayton cycle is compressed, and finally the methane-rich natural gas after heat absorption is used for direct expansion power generation to realize the cascade of LNG cold energyUtilizing; the tower-type concentrating solar heat collector is adopted to convert solar radiation into high-temperature heat energy and supply the high-temperature heat energy as a heat source to supercritical CO2And then the Brayton cycle is compressed, so that the high-efficiency utilization of solar energy is realized.
The invention depends on solar energy as supercritical CO in daytime2The Brayton cycle heat source is compressed again to generate electricity, the waste heat discharged by the Brayton cycle heat source is stored, heat can be continuously provided for the Carlina cycle at night, the problem of uneven solar time distribution is solved, the difficulty of high-temperature heat storage is avoided, the system can reach a continuous power generation state, the effective recovery of C2+ light hydrocarbon resources and the efficient complementary utilization of LNG cold energy and solar energy are realized, and the Brayton cycle heat source has the advantages of reasonable and compact structure, safe and flexible control, high efficiency, energy conservation, strong practicability and low cost.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: 1. an LNG pump; 2. a first tee fitting; 3. a first heat exchanger; 4. a second heat exchanger; 5. a flash column; 6. a demethanizer; 7. a first throttle valve; 8. a deethanizer; 9. a first mixer; 10. a third heat exchanger; 11. a turbo expander; 12. a second throttle valve; 13. a second mixer; 14. a first ammonia pump; 15. a precooler; 16. a separator; 17. An ammonia gas turboexpander; 18. a second ammonia pump; 19. a main compressor; 20. then compressing the mixture; 21. a second tee; 22. a low temperature regenerator; 23. a third mixer; 24. a high temperature regenerator; 25. supercritical CO2A turbo expander; 26. a fourth heat exchanger; 27. a pump; 28. a heat sink; 29. a heliostat.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
Referring to fig. 1, a LNG light hydrocarbon separation coupling supercritical CO2The recompression Brayton/kalina combined cycle power generation system comprises an LNG light hydrocarbon separation system, a light-gathering solar heat collection circulation system and a supercritical CO2Then compressing the Brayton cycle system, the kalina cycle system and the natural gas direct expansion system;
the LNG light hydrocarbon separation system comprises an LNG pump 1, a working medium outlet side of the LNG pump 1 is connected to an inlet side of a first tee joint device 2, an outlet side of the first tee joint device 2 is divided into two branches, wherein, one outlet side is connected with a feeding port I of the demethanizer 6, the other outlet side is connected with a cold flow inlet side of the first heat exchanger 3, a cold flow outlet side of the first heat exchanger 3 is connected with a cold flow inlet side of the second heat exchanger 4, a cold flow outlet side of the second heat exchanger 4 is connected with a feeding port of the flash tower 5, a kettle liquid port of the flash tower 5 is communicated with a feeding port II of the demethanizer 6, a bottom discharge port of the demethanizer 6 is communicated with an inlet side of the first throttle valve 7, an outlet side of the first throttle valve 7 is connected with a feeding port of the deethanizer 8, a top discharge port of the deethanizer 8 is connected with a hot flow inlet side of the second heat exchanger 4, and a top discharge port of the flash tower 5 and a top discharge port of the demethanizer 6 are respectively communicated with two inlet sides of the first mixer 9;
the concentrating solar heat collection circulating system comprises a heliostat 29, the heliostat 29 absorbs sunlight and transfers heat to a heat absorber 28, a working medium outlet side of the heat absorber 28 is communicated with a working medium inlet side of a pump 27, a working medium outlet side of the pump 27 is communicated with a heat flow inlet side of a fourth heat exchanger 26, and a heat flow outlet side of the fourth heat exchanger 26 is communicated with a working medium inlet side of the heat absorber 28;
the supercritical CO2The recompression Brayton cycle system comprises a main compressor 19, wherein the outlet side of the main compressor 19 is communicated with the cold flow inlet side of a low-temperature heat regenerator 22, the cold flow outlet side of the low-temperature heat regenerator 22 and the outlet side of a recompressor 20 are connected into the cold flow inlet side of a high-temperature heat regenerator 24 through a third mixer 23, the cold flow outlet side of the high-temperature heat regenerator 24 is communicated with the cold flow inlet side of a fourth heat exchanger 26, and the cold flow outlet side of the fourth heat exchanger 26 is communicated with the supercritical CO2The inlet side of the turboexpander 25 is connected to supercritical CO2The outlet side of the turboexpander 25 is communicated with the heat flow inlet side of the high-temperature regenerator 24, the heat flow outlet side of the high-temperature regenerator 24 is communicated with the heat flow inlet side of the low-temperature regenerator 22, the heat flow outlet side of the low-temperature regenerator 22 is communicated with the inlet side of the second tee-joint unit 21, the outlet side of the second tee-joint unit 21 is divided into two parts, one part is connected with the inlet side of the recompressor 20, and in addition, the outlet side of the turboexpander 25 is communicated with theOne part is connected to the hot flow inlet side of the precooler 15, and the hot flow outlet side of the precooler 15 is communicated with the inlet side of the main compressor 19;
the kalina circulation system comprises a first ammonia water pump 14, wherein a working medium outlet side of the first ammonia water pump 14 is connected with a cold flow inlet side of a precooler 15, a cold flow outlet side of the precooler 15 is connected with a working medium inlet side of a separator 16, a gas phase outlet end of the separator 16 is communicated with an air inlet of an ammonia gas turbine expander 17, an air outlet of the ammonia gas turbine expander 17 is communicated with a heat flow inlet side of a first heat exchanger 3, a heat flow outlet side of the first heat exchanger 3 is connected with a working medium inlet side of a second ammonia water pump 18, a liquid phase outlet end of the separator 16 is communicated with a heat flow inlet side of a third heat exchanger 10, a heat flow outlet side of the third heat exchanger 10 is connected with an inlet side of a second throttle valve 12, and a working medium outlet side of the second ammonia water pump 18 and an outlet side of the second throttle valve 12 are connected with the working medium inlet side of the first ammonia;
the natural gas direct expansion system comprises a first mixer 9, wherein the outlet side of the first mixer 9 is communicated with the cold flow inlet side of a third heat exchanger 10, and the cold flow outlet side of the third heat exchanger 10 is communicated with the inlet side of a turbine expander 11.
The working medium at the working medium inlet side of the LNG pump 1 is liquefied natural gas.
The working medium at the bottom discharge hole of the deethanizer 8 is liquefied petroleum gas.
And the working medium on the heat flow outlet side of the second heat exchanger 4 is liquid ethane.
The supercritical CO2Recompression of the circulating medium in the Brayton cycle as supercritical CO2。
And the circulating medium in the kalina cycle is an ammonia water mixture.
The outlet side of the turboexpander 11 is directly connected to a user or a company.
The working principle of the invention is as follows: LNG raw materials are pressurized and conveyed to a first tee joint device 2 through an LNG pump 1, the raw materials are divided into two streams of materials with different sizes by the first tee joint device 2, and the larger stream of materials flows through a first heat exchanger 3 and a second heat exchanger 4 to be heated and heated twice and then enters a flash tower5, performing primary separation of methane, directly feeding a smaller stream of material as a reflux liquid into a demethanizer 6, separating the heated LNG raw material into methane-rich natural gas and a kettle liquid rich in C2+ light hydrocarbon resources in the flash tower 5, discharging the methane-rich natural gas from the top of the flash tower 5, feeding the kettle liquid of the flash tower into the demethanizer 6 for further separation, separating the kettle liquid of the flash tower 5 into a natural gas containing high-purity methane and a stream rich in C2+ light hydrocarbon by the demethanizer 6, discharging the methane-rich natural gas from the top of the demethanizer 6 and mixing the methane-rich natural gas discharged from the top of the flash tower 5 in a first mixer 9, then feeding the mixture into a third heat exchanger 10 for heating, throttling and depressurizing the kettle liquid of the demethanizer 6 by a first throttling valve 7 and then feeding the mixture into a deethanizer 8, separating the liquid into a high-purity ethane product, a methane-rich natural gas, and a C2+ light hydrocarbon-rich natural gas, The separated gaseous ethane of the liquefied petroleum gas products such as butane and the like exchanges heat with the LNG raw material in the second heat exchanger 4, so that the gaseous ethane is cooled into liquid ethane, and the light hydrocarbon separation process of the LNG is completed; the heliostat 29 in the light-gathering solar heat collection circulating system synchronously and automatically tracks sunlight, accurately reflects the sunlight to the window of the heat absorber 28, and the gathered light entering the cavity of the heat absorber 28 has high energy density and is used for heating the fused salt working medium flowing through the pipeline of the heat absorber 28 and high-pressure supercritical CO2Exchanging heat with the high-temperature molten salt in the fourth heat exchanger 26, and obtaining the high-temperature high-pressure supercritical CO after heat exchange2By supercritical CO2The turbo expander 25 generates power by applying work, and the applied CO2Enters a high-temperature heat regenerator 24 for constant-pressure heat release to heat CO at the low-temperature side2Then enters a low-temperature heat regenerator 22 for constant pressure heat release; after passing through the low-temperature regenerator 22, a part of CO passes through the second tee joint unit 212The split stream is directed to the recompressor 20 for adiabatic compression, and another portion of the CO2The waste heat is transferred to a kalina circulating system in a precooler 15, and the supercritical CO is precooled by the precooler 152Entering a main compressor 19 for pressurizing, and the pressurized supercritical CO2Enters a low-temperature regenerator 22 for heat absorption and is in contact with CO discharged by a recompressor 202After being mixed, the mixture enters a high-temperature heat regenerator 24 for constant pressure heat absorption, and then exchanges heat with the heated high-temperature molten salt again to finish the heat exchangeSupercritical CO2Recompressing the Brayton cycle; the ammonia water mixture exchanges heat with LNG in the first heat exchanger 3, the condensed ammonia water mixture is mixed with the other part of ammonia water mixture flowing out of the second throttle valve 12 in the second mixer 13, the mixture enters the first ammonia water pump 14 to be pressurized, and the pressurized ammonia water mixture and the high-temperature supercritical CO in the precooler 152Heat exchange, then gas-liquid separation in a separator 16, gas phase in an ammonia gas turbo expander 17 for power generation, ammonia water mixture after power generation enters the first heat exchanger 3 again for condensation, liquid phase containing waste heat exchanges heat with methane-rich natural gas in a third heat exchanger 10, ammonia water mixture after heat exchange enters a second throttle valve 12, ammonia water mixture flowing out of the second throttle valve 12 and ammonia water mixture cooled by the first heat exchanger 3 are mixed in a second mixer 13 again, and kalina cycle is completed; the high-temperature natural gas after exchanging heat with the high-temperature ammonia water mixture in the third heat exchanger 10 drives the turbine expander 11 to do work to generate power, and the direct expansion process of the natural gas is completed.
It should be understood that the above detailed description is only for illustrating the technical solutions of the present invention and is not exhaustive, and although the present invention is described in detail with reference to the above detailed description, a person of ordinary skill in the art should understand that: modifications and equivalents may be made to the embodiments of the invention without departing from the spirit and scope of the invention, which is to be covered by the claims.
Claims (7)
1. Supercritical CO coupling separation of LNG light hydrocarbon2The recompression Brayton/kalina combined cycle power generation system comprises an LNG light hydrocarbon separation system, a light-gathering solar heat collection circulation system and a supercritical CO2Then compressing the Brayton cycle system, the kalina cycle system and the natural gas direct expansion system;
the LNG light hydrocarbon separation system comprises an LNG pump (1), a working medium outlet side of the LNG pump (1) is connected to an inlet side of a first tee joint device (2), an outlet side of the first tee joint device (2) is divided into two branches, wherein one outlet side is connected to a feeding port I of a demethanizer (6), the other outlet side is connected to a cold flow inlet side of a first heat exchanger (3), a cold flow outlet side of the first heat exchanger (3) is connected to a cold flow inlet side of a second heat exchanger (4), a cold flow outlet side of the second heat exchanger (4) is connected to a feeding port of a flash tower (5), a kettle liquid port of the flash tower (5) is communicated with a feeding port II of the demethanizer (6), a bottom discharge port of the demethanizer (6) is communicated with an inlet side of a first throttle valve (7), an outlet side of the first throttle valve (7) is connected to a feeding port of a deethanizer (8), a top discharge port of the deethanizer (8) is connected to a hot flow inlet side of the second heat exchanger (4), a top discharge hole of the flash tower (5) and a top discharge hole of the demethanizer (6) are respectively communicated with two inlet sides of the first mixer (9);
the concentrating solar heat collection circulating system comprises a heliostat (29), the heliostat (29) absorbs sunlight and transfers heat to a heat absorber (28), a working medium outlet side of the heat absorber (28) is communicated with a working medium inlet side of a pump (27), a working medium outlet side of the pump (27) is communicated with a heat flow inlet side of a fourth heat exchanger (26), and a heat flow outlet side of the fourth heat exchanger (26) is communicated with a working medium inlet side of the heat absorber (28);
the supercritical CO2The recompression Brayton cycle system comprises a main compressor (19), wherein the outlet side of the main compressor (19) is communicated with the cold flow inlet side of a low-temperature regenerator (22), the cold flow outlet side of the low-temperature regenerator (22) and the outlet side of a recompressor (20) are connected into the cold flow inlet side of a high-temperature regenerator (24) through a third mixer (23), the cold flow outlet side of the high-temperature regenerator (24) is communicated with the cold flow inlet side of a fourth heat exchanger (26), and the cold flow outlet side of the fourth heat exchanger (26) is communicated with the supercritical CO2The inlet side of the turboexpander (25) is communicated with the supercritical CO2The outlet side of the turboexpander (25) is communicated with the hot flow inlet side of the high-temperature regenerator (24), the hot flow outlet side of the high-temperature regenerator (24) is communicated with the hot flow inlet side of the low-temperature regenerator (22), the hot flow outlet side of the low-temperature regenerator (22) is communicated with the inlet side of a second tee joint (21), the outlet side of the second tee joint (21) is divided into two parts, one part is connected with the inlet side of the recompressor (20), the other part is connected with the hot flow inlet side of the precooler (15), and the hot flow outlet side of the precooler (15) is communicated with the inlet side of the main compressor (19);
the kalina circulation system comprises a first ammonia water pump (14), a working medium outlet side of the first ammonia water pump (14) is connected with a cold flow inlet side of a precooler (15), a cold flow outlet side of the precooler (15) is connected with a working medium inlet side of a separator (16), a gas phase outlet end of the separator (16) is communicated with an air inlet of an ammonia gas turboexpander (17), an air outlet of the ammonia gas turboexpander (17) is communicated with a heat flow inlet side of a first heat exchanger (3), a heat flow outlet side of the first heat exchanger (3) is connected with a working medium inlet side of a second ammonia water pump (18), a liquid phase outlet end of the separator (16) is communicated with a heat flow inlet side of a third heat exchanger (10), and a heat flow outlet side of the third heat exchanger (10) is connected with an inlet side of a second throttle valve (12), the working medium outlet side of the second ammonia pump (18) and the outlet side of the second throttle valve (12) are connected into the working medium inlet side of the first ammonia pump (14) through a second mixer (13);
the natural gas direct expansion system comprises a first mixer (9), wherein the outlet side of the first mixer (9) is communicated with the cold flow inlet side of a third heat exchanger (10), and the cold flow outlet side of the third heat exchanger (10) is communicated with the inlet side of a turboexpander (11).
2. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: the working medium at the working medium inlet side of the LNG pump (1) is liquefied natural gas.
3. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: the working medium at the bottom discharge hole of the deethanizer (8) is liquefied petroleum gas.
4. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: and the working medium on the heat flow outlet side of the second heat exchanger (4) is liquid ethane.
5. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: the supercritical CO2Recompression of the circulating medium in the Brayton cycle as supercritical CO2。
6. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: the circulating medium in the kalina cycle is an ammonia water mixture.
7. The LNG light hydrocarbon separation coupling supercritical CO of claim 12Recompression brayton/kalina combined cycle power generation system its characterized in that: the outlet side of the turboexpander (11) is directly connected to a user or a company.
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