CN105971681A - System and method for utilizing heat of nature - Google Patents
System and method for utilizing heat of nature Download PDFInfo
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- CN105971681A CN105971681A CN201610385466.7A CN201610385466A CN105971681A CN 105971681 A CN105971681 A CN 105971681A CN 201610385466 A CN201610385466 A CN 201610385466A CN 105971681 A CN105971681 A CN 105971681A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
- F01K27/02—Plants modified to use their waste heat, other than that of exhaust, e.g. engine-friction heat
Abstract
The invention belongs to the field of energy utilization, and relates to a method for utilizing heat of the nature, in particular to a system and method for utilizing heat of the nature. The system comprises a compressor, a first expansion machine, a second expansion machine, a heat exchanger and a liquid tank. The compressor, the first expansion machine and the second expansion machine form a driving unit together to be used for outputting mechanical energy to driving machines. The system and method are not only suitable for utilizing the heat of media like air, seawater or terrestrial heat of the nature but also suitable for recycling low-temperature waste heat of factories.
Description
Technical field
The invention belongs to field of energy utilization, the method relating to the Btu utilization of nature, particularly to the system and method for a kind of nature Btu utilization.
Background technology
Nature is filled with the unlimited room temperature energy, an unbounded quantity of room temperature energy such as air, sea water, underground heat, has potentiality to be exploited.The mankind are in the available resource of field of energy utilization, including solar energy, wind energy, seawer tide energy, river water energy, the fossil class energy such as oil, natural gas, coal, nuclear fission, the nuclear energy of nuclear fusion.Although solar energy, wind energy, seawer tide energy, river water energy clean, but the most limited, and can cause Human disturbance naturalness；The fossil class energy such as oil, natural gas, coal, all will result in the rising of global warming, the pollution of air and the rising of atmospheric greenhouse gas carbon dioxide content；Nuclear fission, the energy of nuclear fusion, will result in the rising of global temperatures.
Summary of the invention
Based on this, the present invention provides the system and method for a kind of nature Btu utilization, and the resource conversion utilizing nature is mechanical energy.
Technical solution of the present invention is as follows:
A kind of system of nature Btu utilization, including compressor, described compressor and the connection of the first pressure-control valve, described first pressure-control valve connects with First Heat Exchanger, described First Heat Exchanger is connected by the first pipeline and the second heat exchanger, described second heat exchanger and the connection of the second decompressor, described second decompressor and the connection of the second pressure-control valve, described second pressure-control valve connects with the 3rd heat exchanger, the 4th heat exchanger respectively；
Described 3rd heat exchanger connects with first flow control valve；
Circuit that described 3rd heat exchanger connects with first flow control valve and the 4th heat exchanger parallel communication, the total line of described parallel communication connects with compressor,
Being additionally provided with the 3rd pipeline in the total line of described parallel communication, described 3rd pipeline is provided with the 4th pressure-control valve；
Described 3rd heat exchanger connects with wet tank, described wet tank connects with liquid delivery pump, described liquid delivery pump connects with second flow control valve, described second flow control valve connects with the second heat exchanger, described second heat exchanger is connected with First Heat Exchanger by the second pipeline, described First Heat Exchanger and the connection of the 3rd pressure-control valve, described 3rd pressure-control valve and the connection of the first decompressor, described first decompressor and the connection of the 3rd heat exchanger；
Described compressor, the first decompressor, the second decompressor collectively constitute drive train, to driving machinery output mechanical energy.
System described in employing carries out the method for nature Btu utilization, said method comprising the steps of:
Step 1: the gas of the first working medium by compressor compresses obtain compressor outlet the gas of the first working medium, after being controlled the pressure of the gas of the first working medium after the compression of described compressor outlet by the first pressure-control valve thus controlling the compression of described compressor outlet, the temperature of the gas of the first working medium meets the gasification of the liquid of third party's working medium and the needs of the heat of superheating process；
Step 2: after the compression of described step 1 compressor outlet, the gas of the first working medium obtains the gas of the first working medium after the first pressure-control valve by the first pressure-control valve, the gas of described the first working medium after the first pressure-control valve, through First Heat Exchanger, the second heat exchanger cooling, forms the gas of the first working medium lowered the temperature through heat exchanger；The liquid of third party's working medium is through saturated gas that the second heat exchanger heating and gasifying is third party's working medium, the saturated gas of third party's working medium is heated to be the overheated gas of third party's working medium through First Heat Exchanger, the 3rd pressure-control valve control the pressure of the overheated gas of third party's working medium, second flow control valve control the flow of liquid of third party's working medium thus control the overheated gas temperature of third party's working medium；
Step 3: described step 2 enters, through the gas of the first working medium that heat exchanger is lowered the temperature, the first working medium that the second expander acting obtains the low temperature of the second expander outlet, controlled the first power pressure of the low temperature of described second expander outlet by the second pressure-control valve, while pressure reduces, temperature reduces accordingly；Controlled the pressure of the first working medium of the low temperature of described second expander outlet by the second pressure-control valve, thus control the temperature temperature less than the nature heat source substance chosen of the first working medium of the low temperature of described second expander outlet；
Step 4: the first working medium of the low temperature of described step 3 second expander outlet is divided into two-way, the 4th heat exchanger of leading up to of the first working medium of the low temperature of the second expander outlet is heated by the nature heat source substance chosen, absorb heat, obtain the gas of the first working medium of a road heating；
Step 5: another route first flow control valve of the first working medium of the low temperature of described step 3 second expander outlet is controlled flow, heated to third party's working medium of the first expander outlet by the 3rd heat exchanger, absorb heat, obtain the gas of the first working medium of another road heating；
First working medium of the low temperature of described step 3 second expander outlet converges the gas for the first working medium after converging through the 3rd heat exchanger, the 4th heat exchanger heating；
Step 6: the gas of the first working medium after the converging of described step 5 is supplemented by the 4th pressure-control valve or discharge Stress control, the gas entrance compressor obtaining the first working medium completes the circulation of working medium；
Step 7: in described step 2, the overheated gas of third party's working medium obtains after the overheated gas of third party's working medium of the 3rd pressure valve through the 3rd pressure valve, enters back into the first expander acting；Controlled the pressure of the overheated gas of third party's working medium by the 3rd pressure valve, second flow valve control the flow of liquid of third party's working medium thus control the temperature of the overheated gas of third party's working medium, thus control first expander outlet third party's working medium and connect near-critical subcritical state (temperature, pressure close to and less than critical point)；
Step 8: in described step 5, third party's working medium of the first expander outlet condenses through the 3rd heat exchanger heat exchange, obtains the liquid of third party's working medium of condensation；Another route first flow control valve of first working medium of the low temperature of the second expander outlet controls flow, thus controls cold, and the third party's working medium heat exchange meeting the first expander outlet is condensed into liquid；
Step 9: in described step 8, the liquid of third party's working medium of condensation enters wet tank, the liquid of third party's working medium of described wet tank outlet becomes the highly pressurised liquid of third party's working medium through the pressure-raising of boost in pressure pump, controls to enter the second heat exchanger through second flow control valve, completes the circulation of third party's working medium；
Step 10: compressor, the first decompressor, the second decompressor collectively constitute drive train, output mechanical energy, drive machine operation；4th heat exchanger absorbs the heat of nature heat source substance.
In described step 1, the gas of the first working medium compresses temperature-rise period at least once,
In described step 2, the gas heat exchange temperature-fall period at least once of the first working medium after the first pressure-control valve,
In described step 3, through the gas expansion work temperature-fall period at least once of the first working medium of heat exchanger cooling, complete the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid of third party's working medium gasifies and overheated heating process at least once, completes the first working medium heat transfer process.
In described step 7, the overheated gas of third party's working medium expansion work process at least once, complete the first working medium heat and be converted to the process of mechanical energy.
In described step 4, the first working medium of the low temperature of the second expander outlet absorbs heat process from nature heat source substance at least once, completes the absorption of nature heat；In described step 5, the heat of third party's working medium of the first expander outlet is absorbed by the first working medium of the second expander outlet.
In described step 3, the state of the first working medium of the low temperature of the second expander outlet can be gas or gas-liquid mixture；Third party's working medium state in described step 5, step 7, step 8 can be gas or gas-liquid mixture.
The first selected working medium has the characteristic of the temperature of the nature heat source substance being less than selected absorption heat under room temperature with gas formation existence, boiling point, in order to absorb heat from nature；Selected third party's working medium has low critical temperature, the characteristic of low critical pressure, in order to the gasification of the liquid of third party's working medium is in relative low pressure operation operating mode with overheated, the first decompressor.
The method have the benefit that
1, the present invention is applicable not only to the Btu utilization to media such as nature air, sea water or underground heat, is simultaneously applicable to the recycling of factory's low-temperature waste heat；
2, the present invention can be used for the driving of machinery, it is adaptable to drives electrical power generators, the navigation of boats and ships, the traveling of vehicle, the flight of aircraft, drives electrical power generators process to adapt to the process of refrigerastion of factory, city central air-conditioning refrigeration system, and benefit will be extended.
3, the Btu utilization of the present invention does not only have the discharge of atmospheric greenhouse gas, and do not result in the rising of ambient temperature, energy resource consumption is increased in process of industrialization by the mankind, add carbon-dioxide content in atmosphere, cause the rising of ambient temperature, constraining the mode of mankind's energy resource consumption, application will be the present invention will be addressed.
Accompanying drawing explanation
Fig. 1: present system structural representation；
Wherein: compressor J1, the first decompressor J2, the second decompressor J3, the first pressure-control valve F1, the second pressure-control valve F2, first flow control valve F3, second flow control valve F4, the 3rd pressure-control valve F5, the 4th pressure-control valve F6, First Heat Exchanger E1, the second heat exchanger E2, the 3rd heat exchanger E3, the 4th heat exchanger E4, wet tank V, liquid delivery pump P；
nullThe gas 01 of the first working medium，The gas 02 of the first working medium after the compression of compressor outlet，The gas 03 of the first working medium after the first pressure-control valve，Gas 05 through the first working medium of heat exchanger cooling，First working medium 06 of the low temperature of the second expander outlet，Another road 07 of first working medium of the low temperature of the second expander outlet，One tunnel 08 of the first working medium of the low temperature of the second expander outlet，The gas 09 of the first working medium of another road heating，The gas 10 of the first working medium of one tunnel heating，The gas 11 of the first working medium after converging，The liquid 13 of third party's working medium，The saturated gas 14 of third party's working medium，The overheated gas 15 of third party's working medium，Overheated gas 16 through third party's working medium of the 3rd pressure valve，Third party's working medium 17，The liquid 18 of third party's working medium of condensation，The liquid 19 of third party's working medium of wet tank V outlet.
Detailed description of the invention
Further illustrate the present invention below in conjunction with embodiment, but the scope of protection of present invention is not limited to the scope of embodiment statement.
Embodiment
1
A kind of system of nature Btu utilization, including compressor J1, described compressor J1 and the first pressure-control valve F1 connection, described first pressure-control valve F1 connects with First Heat Exchanger E1, described First Heat Exchanger E1 is connected by the first pipeline and the second heat exchanger E2, described second heat exchanger E2 and the second decompressor J3 connection, described second decompressor J3 and the second pressure-control valve F2 connection, described second pressure-control valve F2 connects with the 3rd heat exchanger E3, the 4th heat exchanger E4 respectively；
Described 3rd heat exchanger E3 connects with first flow control valve F3；
Circuit that described 3rd heat exchanger E3 connects with first flow control valve F3 and the 4th heat exchanger E4 parallel communication, the total line of described parallel communication connects with compressor J1,
Being additionally provided with the 3rd pipeline in the total line of described parallel communication, described 3rd pipeline is provided with the 4th pressure-control valve F6；
Described 3rd heat exchanger E3 connects with wet tank V, described wet tank V connects with liquid delivery pump P, described liquid delivery pump P connects with second flow control valve F4, described second flow control valve F4 and the second heat exchanger E2 connection, described second heat exchanger E2 is connected with First Heat Exchanger E1 by the second pipeline, described First Heat Exchanger E1 and the 3rd pressure-control valve F5 connection, described 3rd pressure-control valve F5 and the first decompressor J2 connection, described first decompressor J2 and the 3rd heat exchanger E3 connection.
Embodiment
2
The method using the system described in embodiment 1 to carry out nature Btu utilization, said method comprising the steps of:
Step 1: the gas 01 of the first working medium by compressor J1 compression obtain compressor outlet the gas 02 of the first working medium, after being controlled the pressure of the gas 02 of the first working medium after the compression of described compressor outlet by the first pressure-control valve F1 thus controlling the compression of described compressor outlet, the temperature of the gas 02 of the first working medium meets the gasification of the liquid 13 of third party's working medium and the needs of the heat of superheating process；
Step 2: after the compression of described step 1 compressor outlet, the gas 02 of the first working medium obtains the gas 03 of the first working medium after the first pressure-control valve by the first pressure-control valve F1, the gas 03 of described the first working medium after the first pressure-control valve, through First Heat Exchanger E1, the second heat exchanger E2 cooling, forms the gas 05 of the first working medium lowered the temperature through heat exchanger；The liquid 13 of third party's working medium is through saturated gas 14 that the second heat exchanger E2 heating and gasifying is third party's working medium, the saturated gas 14 of third party's working medium is heated to be the overheated gas 15 of third party's working medium through First Heat Exchanger E1, the 3rd pressure-control valve F5 control the pressure of the overheated gas 15 of third party's working medium, second flow control valve F4 control the flow of liquid 13 of third party's working medium thus control overheated gas 15 temperature of third party's working medium；
Step 3: described step 2 enters, through the gas 05 of the first working medium that heat exchanger is lowered the temperature, the first working medium 06 that the second decompressor J3 expansion work obtains the low temperature of the second expander outlet, controlled the first working medium 06 pressure of the low temperature of described second expander outlet by the second pressure-control valve F2, while pressure reduces, temperature reduces accordingly；Controlled the pressure of the first working medium 06 of the low temperature of described second expander outlet by the second pressure-control valve F2, thus control the temperature temperature less than the nature heat source substance chosen of the first working medium 06 of the low temperature of described second expander outlet；
Step 4: the first working medium 06 of the low temperature of described step 3 second expander outlet be divided into two-way, one tunnel 08 of the first working medium of the low temperature of the second expander outlet is heated by the nature heat source substance chosen by the 4th heat exchanger E4, absorb heat, obtain the gas 10 of the first working medium of a road heating；
Step 5: another road 07 of the first working medium of the low temperature of described step 3 second expander outlet controls flow by first flow control valve F3, third party's working medium 17 of being exported by the first decompressor J2 by the 3rd heat exchanger E3 is heated, absorb heat, obtain the gas 09 of the first working medium of another road heating；
First working medium 06 of the low temperature of described step 3 second expander outlet converges the gas 11 for the first working medium after converging through the 3rd heat exchanger E3, the 4th heat exchanger E4 heating；
Step 6: the gas 11 of the first working medium after the converging of described step 5 is supplemented by the 4th pressure-control valve F6 or discharged Stress control, obtains the gas 01 of the first working medium and enters compressor J1 and complete the circulation of working medium；
Step 7: in described step 2, the overheated gas 15 of third party's working medium obtains after the overheated gas 16 of third party's working medium of the 3rd pressure valve F5 through the 3rd pressure valve F5, enters back into the first decompressor J2 expansion work；Controlled the pressure of the overheated gas 15 of third party's working medium by the 3rd pressure valve F5, second flow valve F4 control the flow of liquid 13 of third party's working medium thus control the temperature of the overheated gas 15 of third party's working medium, thus control first decompressor J2 outlet third party's working medium 17 and connect near-critical subcritical state (temperature, pressure close to and less than critical point)；
Step 8: in described step 5, third party's working medium 17 of the first decompressor J2 outlet condenses through the 3rd heat exchanger E3 heat exchange, obtains the liquid 18 of third party's working medium of condensation；Another road 07 of first working medium of the low temperature of the second expander outlet is controlled flow by first flow control valve F3, thus controls cold, and the third party's working medium 17 meeting the first decompressor J2 outlet is condensed into liquid；
Step 9: in described step 8, the liquid 18 of third party's working medium of condensation enters wet tank V, the liquid 19 of third party's working medium of described wet tank V outlet becomes the highly pressurised liquid 13 of third party's working medium through the pressure-raising of boost in pressure pump P, controls to enter the second heat exchanger E2 through second flow control valve F4, completes the circulation of third party's working medium；
Step 10: compressor J1, the first decompressor J2, the second decompressor J3 collectively constitute drive train, output mechanical energy, drives machinery E operating；The heat of third party's working medium 17 of the first expander outlet is absorbed by the first working medium of the second expander outlet.
4th heat exchanger E4 absorbs the heat of nature heat source substance.
In described step 1, the gas 01 of the first working medium compresses temperature-rise period at least once,
In described step 2, the gas 03 heat exchange temperature-fall period at least once of the first working medium after the first pressure-control valve,
In described step 3, through the gas 05 expansion work temperature-fall period at least once of the first working medium of heat exchanger cooling, complete the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid 13 of third party's working medium gasifies and overheated heating process at least once, completes the first working medium heat transfer process.
In described step 7, the overheated gas 16 expansion work process at least once of third party's working medium, complete the first working medium heat and be converted to the process of mechanical energy.
In described step 4, the first working medium 06 of the low temperature of the second expander outlet absorbs heat process from nature heat source substance at least once, completes the absorption of nature heat.
In described step 3, the state of the first working medium 06 of the low temperature of the second expander outlet can be gas or gas-liquid mixture；Third party's working medium 17 state in described step 5, step 7, step 8 can be gas or gas-liquid mixture.
Embodiment
3
According to the method described in embodiment 1, wherein:
In described step 1, the gas 01 of the first working medium compresses temperature-rise period at least once,
In described step 2, the gas 03 heat exchange temperature-fall period at least once of the first working medium after the first pressure-control valve,
In described step 3, through the gas 05 expansion work temperature-fall period at least once of the first working medium of heat exchanger cooling, complete the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid 13 of third party's working medium gasifies and overheated heating process at least once, completes the first working medium heat transfer process.
In described step 7, the overheated gas 16 expansion work process at least once of third party's working medium, complete the first working medium heat and be converted to the process of mechanical energy.
In described step 4, the first working medium 06 of the low temperature of the second expander outlet absorbs heat process from nature heat source substance at least once, completes the absorption of nature heat.
In described step 3, the state of the first working medium 06 of the low temperature of the second expander outlet can be gas or gas-liquid mixture；Third party's working medium 17 state in described step 5, step 7, step 8 can be gas or gas-liquid mixture.
Embodiment
4
According to the method described in embodiment 1, wherein:
In described step 1, the gas 01 of the first working medium has 4 second compression temperature-rise periods,
In described step 2, the gas 03 of the first working medium after the first pressure-control valve has 5 heat exchange temperature-fall periods,
In described step 3, the gas 05 through the first working medium of heat exchanger cooling has 1 expansion work temperature-fall period, completes the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid 13 of third party's working medium has 1 gasification and overheated heating process, completes the first working medium heat transfer process.
In described step 7, the overheated gas 16 of third party's working medium has 1 expansion work process, completes the first working medium heat and is converted to the process of mechanical energy.
In described step 4, the first working medium 06 of the low temperature of the second expander outlet have 1 time from nature heat source substance absorb heat process, complete the absorption of nature heat.
In described step 3, the state of the first working medium 06 of the low temperature of the second expander outlet is gas；Third party's working medium 17 state in described step 5, step 7, step 8 is liquid.
Embodiment
5
According to the method described in embodiment 1, wherein:
In described step 1, the gas 01 of the first working medium has 2 second compression processes,
In described step 2, the gas 03 of the first working medium after the first pressure-control valve has 3 heat exchange temperature-fall periods,
In described step 3, the gas 05 through the first working medium of heat exchanger cooling has 4 expansion work temperature-fall periods, completes the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid 13 of third party's working medium has 2 gasifications and overheated heating process, completes the first working medium heat transfer process.
In described step 7, the overheated gas 16 of third party's working medium has 2 expansion work processes, completes the first working medium heat and is converted to the process of mechanical energy.
In described step 4, the first working medium 06 of the low temperature of the second expander outlet have 3 times from nature heat source substance absorb heat process, complete the absorption of nature heat.
In described step 3, the state of the first working medium 06 of the low temperature of the second expander outlet is gas-liquid mixture；Third party's working medium 17 state in described step 5, step 7, step 8 is gas-liquid mixture.
Embodiment
6
According to the method described in embodiment 1, wherein:
In described step 1, the gas 01 of the first working medium has 4 second compression temperature-rise periods,
In described step 2, the gas 03 of the first working medium after the first pressure-control valve has 5 heat exchange temperature-fall periods,
In described step 3, the gas 05 through the first working medium of heat exchanger cooling has 6 expansion work temperature-fall periods, completes the process that temperature raises, heat exports, temperature reduces of the first working medium.
In described step 2, the liquid 13 of third party's working medium has 5 gasifications and overheated heating process, completes the first working medium heat transfer process.
In described step 7, the overheated gas 16 of third party's working medium has 7 expansion work processes, completes the first working medium heat and is converted to the process of mechanical energy.
In described step 4, the first working medium 06 of the low temperature of the second expander outlet have 3 times from nature heat source substance absorb heat process, complete the absorption of nature heat.
In described step 3, the state of the first working medium 06 of the low temperature of the second expander outlet is gas-liquid mixture；Third party's working medium 17 state in described step 5, step 7, step 8 is gas-liquid mixture.
Embodiment
7
According to the method described in embodiment 1, wherein:
The first working medium chosen has the characteristic of the temperature of the nature heat source substance being less than selected absorption heat under room temperature with gas formation existence, boiling point, in order to absorb heat from nature；Selected third party's working medium has low critical temperature, the characteristic of low critical pressure, in order to the gasification of the liquid of third party's working medium is in relative low pressure operation operating mode with overheated, the first decompressor.
Embodiment
8
Using the method that the system described in embodiment 1 carries out nature Btu utilization, the first, the 3rd working medium is now carbon dioxide, and described method includes following:
1000Kmol/ hour, 15 DEG C, the gas 01 of 0.51795Mpa carbon dioxide enter compressor J1, gas 02 pressure of carbon dioxide being controlled compressor J1 outlet by the first pressure-control valve is 5.39Mpa, during gas 02 temperature of compressor outlet carbon dioxide rise a height of 228 DEG C accordingly；
Lowered the temperature through First Heat Exchanger E1, the second heat exchanger E2 heat exchange by the gas 03 of the carbon dioxide of the first pressure-control valve F1, factor due to circulating resistance, pressure, temperature decline, and become 5.35Mpa, the gas 05 of carbon dioxide through heat exchanger cooling of 45 DEG C；
1000Kmol/ hour, 45 DEG C, the gas 05 through the carbon dioxide of heat exchanger cooling of 5.35Mpa enters the second decompressor J3 expansion work, carbon dioxide 06 pressure of the low temperature being controlled the second expander outlet by the second pressure-control valve F2 is 0.53795Mpa, calculate corresponding equivalent temperature and be-111 DEG C, the saturated mode that the carbon dioxide 06 of the low temperature of this second expander outlet coexists for gas-liquid, actual temperature is the carbon dioxide saturation temperature-55.75 DEG C at 0.53795Mpa, liquid CO 2 content therein is 11.63%, and content liquid is by the temperature of the second decompressor J3 entrance carbon dioxide 16, pressure determines；The data of content are all value of calculation, it is proposed that do not make an amendment
The carbon dioxide 06 of the low temperature of the second expander outlet is divided into two-way, one tunnel 08 of the carbon dioxide of the low temperature of the second expander outlet is obtained the gas 10 of the carbon dioxide of a road heating through the 4th heat exchanger E4 by the heating of nature heat source substance, another road 07 of the carbon dioxide of the low temperature of the second expander outlet converges the gas 11 for the carbon dioxide after converging through the gas 09 of the carbon dioxide obtaining the heating of another road of the 3rd heat exchanger E3, the gas 10 of the carbon dioxide of a road heating with the gas 09 of the carbon dioxide of another road heating；In the case of the temperature of nature heat source substance is 30 DEG C, the temperature of the gas 11 of the carbon dioxide after converging is 15 DEG C, and pressure is 0.51795Mpa；Another road 07 of the carbon dioxide of the low temperature of the second expander outlet is controlled flow through the 3rd heat exchanger E3 by first flow control valve F3 thus controls the carbon dioxide 17 of the first decompressor J2 outlet and be in 31 DEG C, the subcritical state of 7.06Mpa (temperature, pressure close to and less than critical point).
The gas 11 of carbon dioxide after the converging of heating, supplementing or discharge by the 4th pressure-control valve F6, thus control the pressure of the gas 01 of compressor J1 entrance carbon dioxide, it is input to compressor J1, completes circulation；
During First Heat Exchanger E1, the second heat exchanger E2 release heat equivalent in the gasification of the liquid CO 2 of 1212 Kmol and overheated heat；
The liquid 18 of the carbon dioxide of the 3rd heat exchanger E3 condensation, its temperature 31 DEG C, pressure 7.06Mpa, enter liquid CO 2 storage tank V；
The liquid 19 of the carbon dioxide of storage tank V output is by pump pressure-raising to 26.2Mpa；
It is 1212Kmol/ hour that liquid CO 2 12 after pump pressure-raising is controlled flow by valve F4, through heat exchanger E1 gasification, through the overheated overheated gas 15 obtaining carbon dioxide of heat exchanger E2, the pressure of overheated gas 15 being controlled carbon dioxide by valve F5 is 25.8Mpa, second flow control valve F4 controlling the flow of the liquid 13 of carbon dioxide thus controlling the temperature of the overheated gas 15 of carbon dioxide is 165 DEG C；
Enter the first expander by the overheated gas 16 of the carbon dioxide of the 3rd pressure-control valve F5 to do work；
1212Kmol/ hour of first decompressor J2 outlet, 7.06Mpa, the carbon dioxide 17 of 31 DEG C obtain the liquid 18 of carbon dioxide of condensation through heat exchanger E3, its pressure is 7.06Mpa, temperature 31 DEG C, enters liquid CO 2 storage tank V, completes circulation；
Carbon dioxide one tunnel 08 pressure of the low temperature of the second expander outlet be 0.53795Mpa ,-55.75 DEG C, containing 11.63% liquid, heated by the nature heat source substance of 30 DEG C through the 4th heat exchanger E4, absorb the heat of 3195668KJ/ hour；
Compressor J1 need to input 7489360KJ/ hour energy, the first decompressor J1 and export 6441161KJ/ hour energy, the second decompressor J2 output 4419105KJ/ hour energy, pump P and need to input 82213KJ/ hour energy, compressor J1, the first decompressor J2, the second decompressor J3 collectively constitute drive train, the energy of exportable 3277881KJ/ hour, corrected performance is 910KW；Output mechanical energy, drives machinery E operating；4th heat exchanger E4 absorbs the heat of nature heat source substance；
The key controlled: the carbon dioxide controlling the first decompressor J2 outlet connects near-critical subcritical state (temperature, pressure are close and are less than critical point), reduce it and be condensed into liberated heat in liquid process, thus increase the 4th heat exchanger E4 heat absorption to nature heat source substance.
4th heat exchanger E4 is from the mechanical energy that the converting heat that nature is drawn is the first decompressor J2 output, can be used for the driving of machinery, it is applicable to drive electrical power generators, the navigation of boats and ships, the traveling of vehicle, the flight of aircraft, driving electrical power generators process to adapt to the process of refrigerastion of factory, city central air-conditioning refrigeration system, benefit will be extended.
The above embodiments are only the preferred technical solution of the present invention, and are not construed as the restriction for the present invention, and the embodiment in the application and the feature in embodiment, can mutual combination in any in the case of not conflicting.The technical scheme that protection scope of the present invention should be recorded with claim, is protection domain including the equivalents of technical characteristic in the technical scheme that claim is recorded.Equivalent the most in this range is improved, also within protection scope of the present invention.
Claims (8)
1. the system of a nature Btu utilization, including compressor (J1), it is characterized in that: described compressor (J1) connects with the first pressure-control valve (F1), described first pressure-control valve (F1) connects with First Heat Exchanger (E1), described First Heat Exchanger (E1) is connected by the first pipeline and the second heat exchanger (E2), described second heat exchanger (E2) connects with the second decompressor (J3), described second decompressor (J3) connects with the second pressure-control valve (F2), described second pressure-control valve (F2) respectively with the 3rd heat exchanger (E3), 4th heat exchanger (E4) connection；
Described 3rd heat exchanger (E3) connects with first flow control valve (F3)；
Circuit that described 3rd heat exchanger (E3) connects with first flow control valve (F3) and the 4th heat exchanger (E4) parallel communication, the total line of described parallel communication connects with compressor (J1),
Being additionally provided with the 3rd pipeline in the total line of described parallel communication, described 3rd pipeline is provided with the 4th pressure-control valve (F6)；
Described 3rd heat exchanger (E3) connects with wet tank (V), described wet tank (V) connects with liquid delivery pump (P), described liquid delivery pump (P) connects with second flow control valve (F4), described second flow control valve (F4) connects with the second heat exchanger (E2), described second heat exchanger (E2) is connected with First Heat Exchanger (E1) by the second pipeline, described First Heat Exchanger (E1) connects with the 3rd pressure-control valve (F5), described 3rd pressure-control valve (F5) connects with the first decompressor (J2), described first decompressor (J2) connects with the 3rd heat exchanger (E3)；
Described compressor (J1), the first decompressor (J2), the second decompressor (J3) collectively constitute drive train, to driving machinery (E) output mechanical energy.
2. use the method that the system described in claim 1 carries out nature Btu utilization, it is characterised in that: said method comprising the steps of:
Step 1: the gas (01) of the first working medium is obtained the gas (02) of the first working medium after the compression of compressor outlet by compressor (J1) compression, after being controlled the pressure of the gas (02) of the first working medium after the compression of described compressor outlet by the first pressure-control valve (F1) thus controlling the compression of described compressor outlet, the temperature of the gas (02) of the first working medium meets the gasification of the liquid (13) of third party's working medium and the needs of the heat of superheating process；
Step 2: the gas (02) of rear first working medium of the compression of described step 1 compressor outlet obtains the gas (03) of the first working medium after the first pressure-control valve by the first pressure-control valve (F1), the gas (03) of described the first working medium after the first pressure-control valve, through First Heat Exchanger (E1), the second heat exchanger (E2) cooling, forms the gas (05) of the first working medium lowered the temperature through heat exchanger；The liquid (13) of third party's working medium is through saturated gas (14) that the second heat exchanger (E2) heating and gasifying is third party's working medium, the saturated gas (14) of third party's working medium is heated to be the overheated gas (15) of third party's working medium through First Heat Exchanger (E1), the 3rd pressure-control valve (F5) control the pressure of the overheated gas (15) of third party's working medium, second flow control valve (F4) control the flow of liquid (13) of third party's working medium thus control overheated gas (15) temperature of third party's working medium；
Step 3: described step 2 enters, through the gas (05) of the first working medium that heat exchanger is lowered the temperature, the first working medium (06) that the second decompressor (J3) expansion work obtains the low temperature of the second expander outlet, controlled the pressure of first working medium (06) of the low temperature of described second expander outlet by the second pressure-control valve (F2), while pressure reduces, temperature reduces accordingly；The first working medium of the low temperature of described second expander outlet is controlled by the second pressure-control valve (F2)
(06) pressure, thus control the temperature temperature less than the nature heat source substance chosen of first working medium (06) of the low temperature of described second expander outlet；
Step 4: the first working medium of the low temperature of described step 3 second expander outlet
(06) be divided into two-way, a road (08) of the first working medium of the low temperature of the second expander outlet is heated by the nature heat source substance chosen by the 4th heat exchanger (E4), absorbs heat, obtains the gas (10) of the first working medium of a road heating；
Step 5: another road (07) of the first working medium of the low temperature of described step 3 second expander outlet is controlled flow, third party's working medium (17) heating exported by the 3rd heat exchanger (E3) by the first decompressor (J2) by first flow control valve (F3), absorb heat, obtain the gas (09) of the first working medium of another road heating；
First working medium (06) of the low temperature of described step 3 second expander outlet converges the gas (11) for the first working medium after converging through the 3rd heat exchanger (E3), the 4th heat exchanger (E4) heating；
Step 6: the gas (11) of the first working medium after the converging of described step 5 is supplemented by the 4th pressure-control valve (F6) or discharge Stress control, the gas (01) entrance compressor (J1) obtaining the first working medium completes the circulation of working medium；
Step 7: in described step 2, the overheated gas (15) of third party's working medium obtains after the overheated gas (16) of third party's working medium of the 3rd pressure valve (F5) through the 3rd pressure valve (F5), enters back into the first decompressor (J2) expansion work；Controlled the pressure of the overheated gas (15) of third party's working medium by the 3rd pressure valve (F5), second flow valve (F4) control the flow of liquid (13) of third party's working medium thus control the temperature of the overheated gas (15) of third party's working medium, thus control the first decompressor (J2) outlet third party's working medium (17) and connect near-critical subcritical state；
Step 8: third party's working medium (17) that in described step 5, first decompressor (J2) exports condenses through the 3rd heat exchanger (E3) heat exchange, obtains the liquid (18) of third party's working medium of condensation；Another road of first working medium of the low temperature of the second expander outlet
(07) being controlled flow by first flow control valve (F3), thus control cold, third party's working medium (17) heat exchange that satisfied first decompressor (J2) exports is condensed into liquid；
Step 9: in described step 8, the liquid (18) of third party's working medium of condensation enters wet tank (V), the liquid (19) of third party's working medium that described wet tank (V) exports becomes the highly pressurised liquid (13) of third party's working medium through the pressure-raising of boost in pressure pump (P), controls to enter the second heat exchanger (E2) through second flow control valve (F4), completes the circulation of third party's working medium；
Step 10: compressor (J1), the first decompressor (J2), the second decompressor (J3) collectively constitute drive train, output mechanical energy, drives machinery (E) operating；4th heat exchanger (E4) absorbs the heat of nature heat source substance.
Method the most according to claim 2, it is characterised in that
In described step 1, the gas (01) of the first working medium compresses temperature-rise period at least once,
In described step 2, gas (03) the heat exchange temperature-fall period at least once of the first working medium after the first pressure-control valve (F1),
In described step 3, through gas (05) the expansion work temperature-fall period at least once of the first working medium of heat exchanger cooling.
Method the most according to claim 2, it is characterised in that:
In described step 2, the liquid (13) of third party's working medium gasifies and overheated heating process at least once.
The method of nature Btu utilization the most according to claim 2, it is characterised in that:
In described step 7, overheated gas (16) the expansion work process at least once of third party's working medium.
The method of nature Btu utilization the most according to claim 2, it is characterised in that
In described step 4, first working medium (06) of the low temperature of the second expander outlet absorbs heat process from nature heat source substance at least once；
In described step 5, the heat of third party's working medium (17) of the first expander outlet is absorbed by the first working medium of the second expander outlet.
The method of nature Btu utilization the most according to claim 2, it is characterised in that: in described step 3, the state of first working medium (06) of the low temperature of the second expander outlet can be gas or gas-liquid mixture；Third party's working medium (17) state in described step 5, step 7, step 8 can be gas or gas-liquid mixture.
Method the most according to claim 2, it is characterised in that: described first working medium has the characteristic of the temperature of the nature heat source substance being less than selected absorption heat under room temperature with gas formation existence, boiling point,；Selected third party's working medium has low critical temperature, the characteristic of low critical pressure.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5680764A (en) * | 1995-06-07 | 1997-10-28 | Clean Energy Systems, Inc. | Clean air engines transportation and other power applications |
| CN1807848A (en) * | 2005-01-20 | 2006-07-26 | 陈祖茂 | Double-fluid steam type double power generation arrangement |
| CN101614139A (en) * | 2009-07-31 | 2009-12-30 | 王世英 | Multicycle power generation thermodynamic system |
| CN203296840U (en) * | 2013-06-06 | 2013-11-20 | 董仲合 | Power machine |
-
2016
- 2016-06-03 CN CN201610385466.7A patent/CN105971681B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5680764A (en) * | 1995-06-07 | 1997-10-28 | Clean Energy Systems, Inc. | Clean air engines transportation and other power applications |
| CN1807848A (en) * | 2005-01-20 | 2006-07-26 | 陈祖茂 | Double-fluid steam type double power generation arrangement |
| CN101614139A (en) * | 2009-07-31 | 2009-12-30 | 王世英 | Multicycle power generation thermodynamic system |
| CN203296840U (en) * | 2013-06-06 | 2013-11-20 | 董仲合 | Power machine |
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