CN114251924A - Endothermic gas liquefaction device and method - Google Patents
Endothermic gas liquefaction device and method Download PDFInfo
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- CN114251924A CN114251924A CN202111100974.3A CN202111100974A CN114251924A CN 114251924 A CN114251924 A CN 114251924A CN 202111100974 A CN202111100974 A CN 202111100974A CN 114251924 A CN114251924 A CN 114251924A
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
本发明提供吸热式气体液化装置，包括气体液化系统、变温装置和冷凝‑蒸发器，所述气体液化系统用于将气体热量转移至冷凝‑蒸发器形成为液态；所述冷凝‑蒸发器中配置有系统工质，用于与气体液化系统进行热交换，系统工质吸收气体液化系统中气体的显热后转变为低温蒸汽；所述变温装置用于将冷凝‑蒸发器中的低温蒸汽转变为高温蒸汽，并将高温蒸汽的部分热量转移,变温装置中高温蒸汽能量转移以后，冷却成液体返回到冷凝‑蒸发器中反复循环。本发明还提供气体液化方法。本发明没有原材料的进出和污染物的产生，对环境气体进行空分。
The invention provides an endothermic gas liquefaction device, comprising a gas liquefaction system, a temperature change device and a condensation-evaporator, the gas liquefaction system is used for transferring the heat of the gas to the condensation-evaporator to form a liquid state; in the condensation-evaporator It is equipped with a system working fluid for heat exchange with the gas liquefaction system, and the system working fluid absorbs the sensible heat of the gas in the gas liquefaction system and transforms into low-temperature steam; the temperature changing device is used to transform the low-temperature steam in the condenser-evaporator It is high temperature steam, and part of the heat of the high temperature steam is transferred. After the energy transfer of the high temperature steam in the temperature changing device, it is cooled into a liquid and returned to the condensing-evaporator for repeated cycles. The present invention also provides a gas liquefaction method. The invention does not have the entry and exit of raw materials and the generation of pollutants, and conducts air separation for ambient gas.
Description
Technical Field
The invention relates to the technical field of energy conversion, in particular to a heat absorption type gas liquefying device and a heat absorption type gas liquefying method.
Background
In the air separation industry, a low-temperature gas liquefaction system is the most energy-consuming system and the main cost of the air separation industry, the best level of the world control is to produce one ton of oxygen at present, the power consumption is about 660 degrees, and the defect of serious energy consumption needs to be improved urgently.
The 1900 Planck proposes that the essence of energy is energy quantum, called quantum for short, any object with thermodynamic temperature of more than absolute 0k has thermodynamic energy, and the essence is energy generated by quantum motion;
E＝TC＝NHV
wherein E is energy, T is thermodynamic temperature, C is specific heat of a substance, the number of N-quanta, H is Planck constant, and V is frequency of quanta.
From the theory, the environment temperature of our people is around 273K, our earth has no more than abundant substances, and the gas available at any time or a lot of gas needing to be compressed is a heat source which is comfortable today, but the existing gas separation technology is that the gas is forcibly compressed mechanically to consume huge energy, the gas is liquefied after the heat in the gas is transferred away by the mechanical compression, and then the gas can be separated.
Disclosure of Invention
In view of one or more of the problems of the prior art, according to one aspect of the present invention, there is provided an endothermic gas liquefaction apparatus comprising a gas liquefaction system, a temperature swing apparatus, and a condenser-evaporator, wherein,
the gas liquefaction system is used for transferring gas heat to the condenser-evaporator to form a liquid state;
the condenser-evaporator is internally provided with a system working medium which is used for exchanging heat with the gas liquefaction system, and the system working medium absorbs the sensible heat of the gas in the gas liquefaction system and then is converted into low-temperature steam;
the temperature changing device is used for converting low-temperature steam in the condensing-evaporating device into high-temperature steam, transferring part of heat of the high-temperature steam, and cooling the high-temperature steam in the temperature changing device into liquid to return to the condensing-evaporating device for repeated circulation after the energy of the high-temperature steam in the temperature changing device is transferred.
Optionally, the gas liquefaction system includes a first blower, a gas cooler, and a liquid pressure pump, the first blower is configured to suck external gas into a high-temperature inlet end of the gas cooler, the liquid pressure pump is configured to suck a system working medium in the condenser-evaporator into a low-temperature inlet end of the gas cooler, the gas sucked by the high-temperature inlet end emits heat to liquefy, and the system working medium sucked by the low-temperature inlet end absorbs the heat emitted by the gas and then returns to the condenser-evaporator.
Optionally, the gas liquefaction system further comprises a gas filter connected in series between the first blower and the high temperature inlet end of the gas cooler.
Optionally, the low temperature outlet end of the gas cooler is in communication with a condenser-evaporator.
Optionally, the heat absorption type gas liquefaction device further comprises a liquid gas pressure pump, wherein the liquid gas pressure pump is communicated with the low-temperature outlet end of the gas cooler through the condenser-evaporator, and is used for sending out the cooled liquid gas after being pressurized through the liquid gas pressure pump, so as to form a low-temperature cold energy generator for cold energy processing.
Optionally, the heat absorption type gas liquefaction device further comprises a fourth heat exchanger, the fourth heat exchanger is communicated with the liquid gas pressurization pump and/or the temperature change device, and is used for collecting heat of external gas and/or converting the pressurized liquid gas into normal-temperature high-pressure gas after absorbing heat in the temperature change device, and then discharging the gas, so as to form the ultra-low energy consumption gas pressurizer.
Optionally, the heat absorption type gas liquefaction device further comprises a cold generator, and the cold generator is communicated with the temperature varying device and is used for converting high-temperature steam of the temperature varying device into electric energy to meet the requirement of the heat absorption type gas liquefaction device per se, outputting the electric energy outwards, and returning generated exhaust gas to the temperature varying device.
Optionally, the endothermic gas liquefaction plant further comprises a gas separation system for separating components from the liquid gas produced by the gas liquefaction system.
Optionally, the gas separation system includes a flash tank that inputs the liquid gas produced by the gas liquefaction system and separates the components of the liquid and gas.
Optionally, the composition of the gas comprises nitrogen.
Optionally, the liquid gas composition further comprises liquid oxygen and liquid argon.
Optionally, the liquid oxygen and liquid argon may be further separated into liquid oxygen and argon again.
Optionally, the gas separation system further comprises a nitrogen compressor, wherein the nitrogen compressor is connected between the flash tank and the condenser-evaporator and is used for pressurizing and conveying the nitrogen separated from the flash tank to the condenser-evaporator to be condensed into liquid again and then conveying the liquid outwards.
Optionally, the gas separation system further includes a liquid gas pressurizing pump, configured to output the mixed liquid gas of the other components after the nitrogen gas is separated from the flash tank to the target object.
Optionally, the temperature varying device includes a heat exchanger mechanism and a second blower, the heat exchange mechanism has a low-pressure loop and a high-pressure loop, an inlet end of the second blower is communicated with the low-pressure loop of the heat exchange mechanism, and an outlet end of the second blower is communicated with the high-pressure loop of the heat exchange mechanism.
Optionally, the heat exchange mechanism comprises a recuperative heat exchanger, a first heat exchanger and a second heat exchanger, the recuperative heat exchanger, the second heat exchanger and the second blower being connected in series, the first heat exchanger being connected in parallel with the second heat exchanger.
Optionally, the temperature varying device further comprises a temperature regulating valve, which is configured in the high-pressure loop of the temperature varying device and is used for controlling the flow distribution of the high-temperature and high-pressure steam output by the blower between the first heat exchanger and the second heat exchanger, so as to control the temperature range of the high-temperature steam output by the first heat exchanger.
Optionally, the heat exchange mechanism further comprises a third heat exchanger for increasing the temperature difference between the high-pressure circuit and the low-pressure circuit at the high-temperature end of the second heat exchanger.
Optionally, the second blower and/or the first heat exchanger and/or the second heat exchanger and/or the third heat exchanger are provided with an insulation layer.
According to another aspect of the present invention, there is provided a method for liquefying gas by the endothermic gas liquefaction apparatus, comprising:
transferring the gas heat to a condenser-evaporator through a gas liquefaction system to form a liquid state;
the system working medium in the condenser-evaporator exchanges heat with the gas liquefaction system, and the system working medium absorbs the sensible heat of the gas in the gas liquefaction system and then is converted into low-temperature steam;
the low-temperature steam in the condensing-evaporator is converted into high-temperature steam through the temperature changing device, part of heat of the high-temperature steam is transferred, and after the energy of the high-temperature steam in the temperature changing device is transferred, the high-temperature steam is cooled into liquid which returns to the condensing-evaporator for repeated circulation.
Optionally, the step of transferring the heat of the gas to the liquid state by the gas liquefaction system to the condenser-evaporator further comprises:
cooling the liquid gas by a condenser-evaporator;
pressurizing the cooled liquid gas by a liquid gas pressurizing pump and then sending the pressurized liquid gas out to form a low-temperature cold energy generator for cold energy processing;
and pressurizing the cooled liquid gas by a liquid gas pressurizing pump, then sending the pressurized liquid gas into a fourth heat exchanger, acquiring the heat of external gas by the fourth heat exchanger, or converting the pressurized liquid gas into normal-temperature high-pressure gas after absorbing the heat of the first heat exchanger in the temperature changing device, and discharging to form the ultralow-energy-consumption gas pressurizer.
Optionally, the step of transferring the heat of the gas to the liquid state by the gas liquefaction system to the condenser-evaporator further comprises:
the gas component with lower gasification temperature in the liquid gas is separated by a gas separation system.
Optionally, the step of transferring a portion of the heat of the high temperature steam comprises:
converting part of high-temperature steam of the temperature changing device into electric energy through a cold power generator;
and returning exhaust gas generated by the cold power generator to the temperature changing device.
The heat absorption type gas liquefaction device and the method do not generate the in-out of raw materials and pollutants, air is ubiquitous, small in size, light in weight and low in cost, can meet the requirements of gas liquefaction or air separation of most of fixed or mobile loads on the spot and energy requirements, and provide sufficient foundation guarantee for the whole human society to realize comprehensive electrification.
The heat absorption type gas liquefaction device and the method change the gas liquefaction device from a high energy consumption device into power generation equipment, fundamentally and permanently solve the energy problem caused by the need of more gas separation in the process of human progress, simultaneously solve the problems of carbon emission and air pollution, and have great significance for the development of the current society.
Drawings
FIG. 1 is a schematic view of a first embodiment of an endothermic gas liquefaction plant according to the present invention;
FIG. 2 is a schematic view of a second embodiment of an endothermic gas liquefaction plant according to the present invention;
FIG. 3 is a schematic view of a third embodiment of an endothermic gas liquefaction plant according to the present invention;
FIG. 4 is a schematic view of a fourth embodiment of an endothermic gas liquefaction train according to the present invention;
icon: 1-a condenser-evaporator, 1 a-a first low-temperature outlet end of the condenser-evaporator, 1 b-a second low-temperature outlet end of the condenser-evaporator, 1 c-a first high-temperature inlet end of the condenser-evaporator, 1 d-a second high-temperature inlet end of the condenser-evaporator, 1 e-a high-temperature outlet end of the condenser-evaporator, 1 f-a low-temperature inlet end of the condenser-evaporator, 2-a temperature varying device, 2 a-a low-temperature inlet end of the temperature varying device, 2 b-a low-temperature outlet end of the temperature varying device, 2 c-a low-pressure loop input end of the temperature varying device, 2 d-a high-pressure loop output end of the temperature varying device, 3-a first heat exchanger, 4-a regenerative heat exchanger, 5-a high-pressure loop, 6-a low-pressure loop, 7-second heat exchanger, 71-third heat exchanger, 8-second blower, 8 a-second blower inlet end, 8 b-second blower outlet end, 9-temperature regulating valve, 10-liquid pressure pump, 10 a-low pressure inlet end of liquid pressure pump, 10 b-high pressure outlet end of liquid pressure pump, 11-cold power generator, 11 a-high pressure inlet end of cold power generator, 11 b-low pressure outlet end of cold power generator, 12-gas cooler, 12 a-high temperature inlet end of gas cooler, 12 b-low temperature outlet end of gas cooler, 12 c-low temperature inlet end of gas cooler, 12 d-high temperature outlet end of gas cooler, 13-gas filter, 14-first blower, 15-liquid gas pressure pump, 15 a-a low pressure inlet end of the liquid gas booster pump, 15 b-a high pressure outlet end of the liquid gas booster pump, 16-a nitrogen compressor, 17-a flash tank, 17 a-an inlet end of the flash tank, 17 b-a flash nitrogen outlet of the flash tank, 17 c-a liquid gas outlet of the flash tank, 18-a fourth heat exchanger, 18 a-a low temperature inlet end of the fourth heat exchanger, 18 b-a high temperature outlet end of the fourth heat exchanger, 18 c-a high temperature inlet end of the fourth heat exchanger, 18 d-a low temperature outlet end of the fourth heat exchanger.
Detailed Description
The terms "first," "second," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be further noted that unless otherwise explicitly stated or limited, the terms "disposed," "mounted," "connected," and "connected" should be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Fig. 1 is a schematic view of a first embodiment of the endothermic gas liquefaction apparatus according to the present invention, as shown in fig. 1, the endothermic gas liquefaction apparatus includes a gas liquefaction system including a first blower 14, a gas filter 13, a gas cooler 12, a liquid pressurizing pump 10, a liquid gas pressurizing pump 15, and a fourth heat exchanger 18, a temperature changing device 2, and a condenser-evaporator 1, the first blower 14 sucks and pressurizes an external gas to enable the external gas to flow against an on-way resistance, and the gas filter 13 separates dust particles, volatile gas, moisture, and carbon dioxide in the external gas, ensures cleanliness of the air-separated gas and prevents frosting during cooling, while achieving collection of moisture and capture of carbon dioxide; the liquid pressure pump 10 is used for pressurizing a system working medium and then flowing into the gas cooler 12; the gas cooler 12 is used for cooling the filtered external gas to release heat and converting the heat into liquid gas, and the system working medium flowing through the gas cooler 12 absorbs the heat and returns to the condenser-evaporator 1; the condenser-evaporator 1 is provided with a system working medium and is used for carrying out heat exchange with the liquid gas sent by the gas cooler 12 and the returned system working medium after absorbing heat, the liquid gas is further cooled and then sent to a liquid gas pressure pump, and the system working medium in the condenser-evaporator 1 is converted into low-temperature steam and sent to the temperature changing device 2; the temperature changing device 2 is used for converting low-temperature steam into high-temperature steam, and after the energy of the high-temperature steam is transferred, the high-temperature steam is cooled into liquid and returns to the condenser-evaporator 1; the liquid gas pressurizing pump 15 is used for pressurizing the liquid gas after the condenser-evaporator 1 is further cooled and sending the liquid gas into the fourth heat exchanger 18; the fourth heat exchanger 18 is configured to collect heat of the external air, and convert the heat absorbed by the pressurized liquid air into a normal-temperature high-pressure gas, and discharge the normal-temperature high-pressure gas.
In one embodiment, as shown in fig. 1, the first blower 14 is connected to the high temperature inlet end 12a of the gas cooler 12 through a gas filter 13, the low temperature outlet end 12b of the gas cooler 12 is connected to the first high temperature inlet end 1c of the condenser-evaporator 1, the first low temperature outlet end 1a of the condenser-evaporator 1 is connected to the low pressure inlet end 15a of the liquid gas pressure pump 15, the high pressure outlet end 15b of the liquid gas pressure pump 15 is connected to the low temperature inlet end 18a of the fourth heat exchanger 18, the high temperature inlet end 18c and the low temperature outlet end 18d of the fourth heat exchanger 18 are respectively connected to the low temperature outlet end 2b and the low temperature inlet end 2a of the temperature varying device, so as to convert the pressurized liquid air into the normal temperature and high pressure gas through the high temperature outlet end 18b of the fourth heat exchanger, the second low-temperature outlet end 1b of the condenser-evaporator 1 is communicated with the low-pressure inlet end 10a of the liquid booster pump 10, the high-pressure outlet end 10b of the liquid booster pump 10 is communicated with the low-temperature inlet end 12c of the gas cooler 12, the high-temperature outlet end 12d of the gas cooler 12 is communicated with the second high-temperature inlet end 1d of the condenser-evaporator 1, the high-temperature outlet end 1e of the condenser-evaporator 1 is communicated with the low-pressure loop 6 of the temperature varying device 2, and the low-temperature inlet end 1f of the condenser-evaporator 1 is communicated with the high-pressure loop 5 of the temperature varying device 2.
The method for liquefying gas by the endothermic gas liquefaction device comprises the following steps:
step S1, sucking external air by the first blower 14, pressurizing the air, and introducing the air into the air filter 13;
step S11, filtering the outside air through the air filter 13;
step S12, cooling the filtered outside air by the gas cooler 12 to convert the cooled outside air into liquid gas, and releasing heat energy;
step S2, pressurizing the system working medium by the liquid pressure pump 10 and then entering the gas cooler 12;
step S3, the working medium of the high-pressure system flowing through the gas cooler 12 and the step S2 absorbs the heat energy released in the step S12 and converts the heat energy into high-temperature high-pressure liquid, the high-temperature high-pressure liquid returns to the condensing-evaporating unit 1, and the released heat is converted into low-temperature liquid;
step S4, further cooling the liquid gas by the condenser-evaporator 1, releasing heat energy;
step S41, the further cooled liquid gas is pressurized by the liquid gas pressurizing pump 15 and then sent to the fourth heat exchanger 18;
step S42, absorbing the high-temperature heat in the temperature varying device by the fourth heat exchanger 18 to convert the pressurized liquid gas into a normal-temperature high-pressure gas, and discharging the gas;
step S5, absorbing the heat energy released in step S3 and step S4 by the system working medium in the condenser-evaporator, converting the heat energy into low-temperature steam, and entering the temperature changing device 2;
step S6, converting the low-temperature steam into high-temperature steam through the temperature changing device 2, and cooling the high-temperature steam into liquid to return to the condenser-evaporator 1 after the energy of the high-temperature steam is transferred;
step S7, loop through step S1-step S6.
The heat absorption type gas liquefaction device transfers the heat in the gas in a non-mechanical compression mode, so that the gas is liquefied and then pressurized and heated to form the gas compressor with ultra-low energy consumption.
In the embodiment, the purpose of outputting electric energy is not taken, only gas pressurization is taken as a target, so that the energy of air is transferred to liquefied air and then the liquefied air is pressurized, then the temperature of the transferred air energy is raised by using a temperature changing device, and the liquefied pressurized liquid is heated to achieve high-pressure normal-temperature air, and the heat absorption type gas liquefying device only needs to provide little electric energy, so that an ideal isenthalpic compressor is connected.
The embodiment is suitable for pressurization of any gas at any temperature, such as pressurization in natural gas transmission, liquefaction of gas in the process of loading natural gas into a ship, recompression liquefaction after liquid gasification of a natural gas storage tank, a high-pressure blower of an iron-making blast furnace and the like.
Fig. 2 is a schematic view of a second embodiment of the endothermic gas liquefaction apparatus of the present invention, as shown in fig. 2, the endothermic gas liquefaction apparatus comprises a gas liquefaction system including a first blower 14, a gas filter 13, a gas cooler 12, a liquid pressurization pump 10, and a liquid gas pressurization pump 15, a temperature change apparatus 2, a condenser-evaporator 1, and a cold power generator, the first blower 14 is used for sucking and pressurizing an external gas, and the gas filter 13 is used for filtering a high-pressure external gas sent from the first blower 14; the liquid pressure pump 10 is used for pressurizing a system working medium and then flowing into the gas cooler 12; the gas cooler 12 is used for cooling the filtered external gas to release heat and convert the heat into liquid gas, and a high-pressure system working medium flowing through the gas cooler 12 absorbs the heat and converts the heat into high-temperature high-pressure liquid which is transmitted to the temperature changing device 2; the condenser-evaporator 1 is provided with a system working medium and is used for carrying out heat exchange with the liquid gas sent by the gas cooler 12, the liquid gas is further cooled and then sent to a liquid gas adding pump, and the system working medium in the condenser-evaporator 1 is converted into low-temperature steam and sent to the temperature changing device 2; the liquid gas pressure pump 15 is used for pressurizing and discharging the liquid gas after the condenser-evaporator 1 is further cooled; the temperature changing device 2 is used for converting low-temperature steam sent by the condenser-evaporator 1 into high-temperature steam, the energy of the high-temperature steam is transferred to high-pressure liquid sent by the gas cooler 12, the high-pressure liquid is converted into high-temperature high-pressure steam and sent to the cold power generator 11, and the high-temperature steam is cooled into liquid and returns to the condenser-evaporator 1; the cold power generator 11 is used for converting the high-temperature high-pressure steam sent by the temperature varying device 2 into electric energy and returning the generated exhaust gas to the temperature varying device 2.
In one embodiment, as shown in fig. 2, the first blower 14 is connected to the high temperature inlet end of the gas cooler 12 through a gas filter 13, the low temperature outlet end of the gas cooler 12 is connected to the first high temperature inlet end 1c of the condenser-evaporator 1, the first low temperature outlet end 1a of the condenser-evaporator 1 is connected to the low pressure inlet end of the liquid gas pressure pump 15, the second low temperature outlet end 1b of the condenser-evaporator 1 is connected to the low pressure inlet end of the liquid pressure pump 10, the high pressure outlet end of the liquid pressure pump 10 is connected to the low temperature inlet end of the gas cooler 12, the high temperature outlet end of the gas cooler 12 is connected to the low temperature inlet end 2a of the temperature changing device 2, the low temperature outlet end 2b of the temperature changing device 2 is connected to the high pressure inlet end 11a of the cold power generator 11, the low pressure outlet end 11b of the cold power generator 11 is connected to the low pressure loop input end 2c of the temperature changing device 2, the high-temperature outlet end of the condenser-evaporator 1 is communicated with the input end of the low-pressure loop of the temperature varying device 2, and the low-temperature inlet end of the condenser-evaporator 1 is communicated with the output end 2d of the high-pressure loop of the temperature varying device 2.
The method for liquefying gas by the endothermic gas liquefaction device comprises the following steps:
step S10, sucking external air by the first blower 14, pressurizing the air, and introducing the air into the air filter 13;
step S101, filtering the outside air through the air filter 13;
step S102, cooling the filtered external gas by the gas cooler 12 to convert the external gas into liquid gas and release heat energy;
step S20, pressurizing the system working medium by the liquid pressure pump 10 and then entering the gas cooler 12;
step S30, the system working medium flowing through the gas cooler 12 in step S20 absorbs the heat energy released in step S102 and converts the heat energy into high-temperature high-pressure liquid, and the high-temperature high-pressure liquid is transmitted to the temperature changing device 2;
step S40, further cooling the liquid gas of step S102 by the condenser-evaporator 1, releasing heat energy;
step S401, the further cooled liquid gas is pressurized by the liquid gas pressurizing pump 15 and then discharged and conveyed to a target object (low-temperature gas supply), so as to form an ultra-low temperature cold energy generator;
step S50, absorbing the heat energy released in the step S40 by the system working medium in the condenser-evaporator, converting the heat energy into low-temperature steam, and entering the temperature changing device 2;
step S60, converting the low-temperature steam into high-temperature steam through the temperature changing device 2, transferring the energy of the high-temperature steam to the high-temperature high-pressure liquid in the step S30, converting the high-temperature high-pressure liquid into high-temperature high-pressure steam, and enabling the high-temperature high-pressure steam to enter the cold power generator 11;
step S70, converting heat energy into electric energy through the cold power generator 11, returning the generated exhaust gas to the condenser-evaporator 1, absorbing the heat energy of the exhaust gas by a system working medium in the condenser-evaporator 1 to generate low-temperature steam, reducing the temperature of the exhaust gas to convert the exhaust gas into liquid, and converting the exhaust gas into high-temperature high-pressure steam through the liquid pressure pump 10, the gas cooler 12 and the temperature changing device 2 to return to the cold power generator 11;
step S80, loop through step S10-step S70.
The heat absorption type gas liquefaction device converts heat energy transferred from gas into electric energy and heat energy, so that the energy consumption device becomes a zero-carbon power supply device.
The endothermic gas liquefaction device described above feeds the liquefied gas into a condenser-evaporator to be further cooled, and then pressurizes it again, and supplies the low-temperature liquid after pressure increase directly to a desired target (low-temperature gas supply such as low-temperature pulverization of rubber or plastic).
Fig. 3 is a schematic view of a third embodiment of the endothermic gas liquefaction apparatus according to the present invention, as shown in fig. 3, the endothermic gas liquefaction apparatus includes a gas liquefaction system including a first blower 14, a gas filter 13, a gas cooler 12, a liquid pressurization pump 10, a liquid gas pressurization pump 15, and a fourth heat exchanger 18, a temperature change apparatus 2, a condenser-evaporator 1, and a cold power generator 11, the first blower 14 is used for sucking and pressurizing external gas, and the gas filter 13 is used for filtering high-pressure external gas sent from the first blower 14; the liquid pressure pump 10 is used for pressurizing a system working medium and then flowing into the gas cooler 12; the gas cooler 12 is used for cooling the filtered external gas to release heat and convert the heat into liquid gas, and a high-pressure system working medium flowing through the gas cooler 12 absorbs the heat and converts the heat into high-temperature high-pressure liquid which is transmitted to the temperature changing device 2; the condenser-evaporator 1 is provided with a system working medium and is used for carrying out heat exchange with the liquid gas sent by the gas cooler 12, the liquid gas is further cooled and then sent to a liquid gas adding pump, and the system working medium in the condenser-evaporator 1 is converted into low-temperature steam and sent to the temperature changing device 2; the liquid gas pressurizing pump 15 is used for pressurizing the liquid gas after the condenser-evaporator 1 is further cooled and sending the liquid gas into the fourth heat exchanger 18; the high-temperature inlet end 18c and the low-temperature outlet end 18d of the fourth heat exchanger 18 are used for collecting heat of external air, and the pressurized liquid air absorbs the heat and is converted into normal-temperature high-pressure air to be discharged; the temperature changing device 2 is used for converting low-temperature steam sent by the condenser-evaporator 1 into high-temperature steam, transferring the energy of the high-temperature steam to high-temperature high-pressure liquid sent by the gas cooler 12, converting the high-temperature high-pressure liquid into high-temperature high-pressure steam and sending the high-temperature high-pressure steam to the cold power generator 11, and cooling the high-temperature steam into liquid which returns to the condenser-evaporator 1; the cold power generator 11 is used for converting the high-temperature high-pressure steam sent by the temperature varying device 2 into electric energy and returning the generated exhaust gas to the temperature varying device 2.
In one embodiment, as shown in fig. 3, the first blower 14 is connected to the high temperature inlet end of the gas cooler 12 through a gas filter 13, the low temperature outlet end of the gas cooler 12 is connected to the first high temperature inlet end 1c of the condenser-evaporator 1, the first low temperature outlet end 1a of the condenser-evaporator 1 is connected to the low pressure inlet end of a liquid gas pressure pump 15, the high pressure outlet end of the liquid gas pressure pump 15 is connected to the low temperature inlet end of a fourth heat exchanger 18, the second low temperature outlet end 1b of the condenser-evaporator 1 is connected to the low pressure inlet end of a liquid pressure pump 10, the high pressure outlet end of the liquid pressure pump 10 is connected to the low temperature inlet end of the gas cooler 12, the high temperature outlet end of the gas cooler 12 is connected to the low temperature inlet end of the temperature changing device 2, and the low temperature outlet end of the temperature changing device 2 is connected to the high pressure inlet end of the cold power generator 11, the low-pressure outlet end of the cold power generator 11 is communicated with the input end of the low-pressure loop of the temperature varying device 2, the high-temperature outlet end of the condenser-evaporator 1 is communicated with the input end of the low-pressure loop of the temperature varying device 2, and the low-temperature inlet end of the condenser-evaporator 1 is communicated with the output end of the high-pressure loop of the temperature varying device 2.
The method for liquefying gas by the endothermic gas liquefaction device comprises the following steps:
step S100, sucking external air by a first blower 14, pressurizing the external air, and then introducing the external air into a gas filter 13;
step S110 of filtering the outside air through the air filter 13;
step S120, cooling the filtered external gas by the gas cooler 12 to convert the external gas into liquid gas and release heat energy;
step S200, pressurizing a system working medium by a liquid pressurizing pump 10 and then feeding the system working medium into a gas cooler 12;
step S300, the system working medium flowing through the gas cooler 12 and the step S200 absorbs the heat energy released in the step S120 and converts the heat energy into high-temperature high-pressure liquid, and the high-temperature high-pressure liquid is transmitted to the temperature changing device 2;
step S400, further cooling the liquid gas of step S120 through the condenser-evaporator 1, releasing heat energy;
step S410, pressurizing the further cooled liquid gas by a liquid gas pressurizing pump 15, and then sending the gas into a fourth heat exchanger 18;
step S420, collecting heat in the external environment through the fourth heat exchanger 18, converting the pressurized liquid gas into normal-temperature high-pressure gas, and discharging the gas to form a zero-carbon gas compression power generation system;
step S500, absorbing the heat energy released in the step S400 by the system working medium in the condensation-evaporation tank, converting the heat energy into low-temperature steam, and entering the temperature changing device 2;
step S600, low-temperature steam is converted into high-temperature steam through the temperature changing device 2, the energy of the high-temperature steam is transferred to the high-temperature high-pressure liquid in the step S300, and the high-temperature high-pressure liquid is converted into high-temperature high-pressure steam and enters the cold power generator 11;
step S700, converting heat energy into electric energy through the cold power generator 11, returning the generated exhaust gas to the condenser-evaporator 1, absorbing the heat energy of the exhaust gas by a system working medium in the condenser-evaporator 1 to generate low-temperature steam, reducing the temperature of the exhaust gas to convert the exhaust gas into liquid, and converting the exhaust gas into high-temperature high-pressure steam through the liquid pressure pump 10, the gas cooler 12 and the temperature changing device 2 to return to the cold power generator 11;
and step S800, looping the steps S100 to S700.
The system is characterized in that the gas is liquefied and then is not required to be separated, only the gas is required to be pressurized, the liquefied gas can be sent into the condenser-evaporator 1 for cryogenic cooling again according to needs, then the liquefied gas is pressurized to a target pressure through the liquid gas pressurizing pump 15, and the liquid is heated and gasified through the fourth heat exchanger 18 to become the normal-temperature high-pressure gas, so that zero-carbon isenthalpic compression (gas liquefaction pressurization heating power generation compressor) is realized.
Fig. 4 is a schematic view showing a fourth embodiment of the endothermic gas liquefaction apparatus according to the present invention, which comprises a gas liquefaction system including a first blower 14, a gas filter 13, a gas cooler 12, a liquid pressurizing pump 10, a flash tank 17, a nitrogen compressor 16, and a liquid gas pressurizing pump 15, a temperature varying apparatus 2, a condenser-evaporator 1, and a cold power generator 11, wherein the first blower 14 sucks and pressurizes the external gas to overcome the on-way resistance and enable the external gas to flow, and the gas filter 13 separates dust particles, volatile gas, moisture, and carbon dioxide in the external gas, ensures the cleanliness of the air-separated gas and prevents frosting during cooling, and simultaneously enables collection of moisture and capture of carbon dioxide, as shown in fig. 4; the liquid pressure pump 10 is used for pressurizing a system working medium and then flowing into the gas cooler 12; the gas cooler 12 is used for cooling the filtered external gas to release heat and convert the heat into liquid gas, and the system working medium flowing through the gas cooler 12 absorbs the heat and converts the heat into high-temperature high-pressure liquid to be transmitted to the temperature changing device 2; the condenser-evaporator 1 is provided with a system working medium and is used for carrying out heat exchange with the liquid gas fed by the gas cooler 12, the liquid gas is further cooled and then fed into the flash tank 17, and the system working medium in the condenser-evaporator 1 is converted into low-temperature steam and fed into the temperature changing device 2; the flash tank 17 is used for inputting the liquid gas cooled by the gas cooler 12 and separating liquid and gas components, preferably, the gas component comprises nitrogen, and preferably, the liquid gas component further comprises liquid oxygen and liquid argon; the nitrogen compressor 16 is connected between the flash tank 17 and the condenser-evaporator 1, and is used for pressurizing and conveying the nitrogen separated from the flash tank 17 to the condenser-evaporator 1 to be condensed into liquid again, and then conveying the liquid outwards; the liquid gas pressure pump 15 is configured to output the mixed liquid gas of the other components after the nitrogen gas is separated from the flash tank 17 to a target object, where the target object may be the flash tank 17 (oxygen and argon are separated by flash again), an external environment, an external device, or the like; the temperature changing device 2 is used for converting low-temperature steam sent by the condenser-evaporator 1 into high-temperature steam, the energy of the high-temperature steam is transferred to high-pressure liquid sent by the gas cooler 12, the high-pressure liquid is converted into high-temperature high-pressure steam and sent to the cold power generator 11, and the high-temperature steam is cooled into liquid and returns to the condenser-evaporator 1; the cold power generator 11 is used for converting the high-temperature high-pressure steam sent by the temperature varying device 2 into electric energy and returning the generated exhaust gas to the temperature varying device 2.
In one embodiment, as shown in fig. 4, the first blower 14 is connected to the high temperature inlet end of the gas cooler 12 through the gas filter 13, the low temperature outlet end of the gas cooler 12 is connected to the inlet end 17a of the flash tank 17, the flash nitrogen outlet 17b of the flash tank 17 is connected to the first high temperature inlet end 1c of the condenser-evaporator 1 through the nitrogen compressor 16, the liquid gas outlet 17c of the flash tank 17 is connected to the liquid gas pressurizing pump 15, the first low temperature outlet end 1a of the condenser-evaporator 1 discharges nitrogen gas, the second low temperature outlet end 1b of the condenser-evaporator 1 is connected to the low pressure inlet end of the liquid pressurizing pump 10, the high pressure outlet end of the liquid pressurizing pump 10 is connected to the low temperature inlet end of the gas cooler 12, the high temperature outlet end of the gas cooler 12 is connected to the low temperature inlet end of the temperature changing device 2, the low-temperature outlet end of the temperature changing device 2 is communicated with the high-pressure inlet end of the cold power generator 11, the low-pressure outlet end of the cold power generator 11 is communicated with the low-pressure loop input end of the temperature changing device 2, the high-temperature outlet end of the condensation-evaporator 1 is communicated with the low-pressure loop input end of the temperature changing device 2, and the low-temperature inlet end of the condensation-evaporator 1 is communicated with the high-pressure loop output end of the temperature changing device 2.
The method for liquefying gas by the endothermic gas liquefaction device comprises the following steps:
step S1000, sucking external air by a first blower 14, pressurizing the external air, and then introducing the external air into a gas filter 13;
step S1001 of filtering the outside air through the air filter 13;
step S1002, cooling the filtered external gas by the gas cooler 12 to release heat energy and convert the heat energy into liquid gas;
step S2000, pressurizing the system working medium by the liquid pressurizing pump 10 and then feeding the system working medium into the gas cooler 12;
step S3000, the system working medium flowing through the gas cooler 12 and released in the step S2000 absorbs the heat energy released in the step S1002 and converts the heat energy into high-temperature high-pressure liquid, and the high-temperature high-pressure liquid is transmitted to the temperature changing device 2;
step S4000, feeding the liquid gas of step S1002 into a flash tank 17, separating liquid and gas components by the flash tank 17, pressurizing the gas components by a nitrogen compressor 16, feeding the gas components to a condenser-evaporator 1, further cooling the gas components into liquid nitrogen, and externally conveying the liquid nitrogen; the components of the liquid are externally output to a target object through a liquid gas pressurizing pump 15;
step S5000, absorbing the heat energy released in the step S4000 by the system working medium in the condensation-evaporation tank, converting the heat energy into low-temperature steam, and entering a temperature changing device 2;
step S6000, converting the low-temperature steam into high-temperature steam through the temperature changing device 2, transferring the energy of the high-temperature steam to the high-temperature high-pressure liquid in the step S3000, converting the high-temperature high-pressure liquid into high-temperature high-pressure steam, and enabling the high-temperature high-pressure steam to enter the cold power generator 11;
step S7000, converting heat energy into electric energy through the cold power generator 11, returning the generated exhaust gas to the condenser-evaporator 1, absorbing the heat energy of the exhaust gas by a system working medium in the condenser-evaporator 1 to generate low-temperature steam, reducing the temperature of the exhaust gas to convert the exhaust gas into liquid, and converting the exhaust gas into high-temperature high-pressure steam through the liquid pressure pump 10, the gas cooler 12 and the temperature changing device 2 to return to the cold power generator 11;
step S8000, loop step S1000-step S7000.
The heat absorption type gas liquefaction device is used for separating various gases and outputting corresponding liquid products by flashing, cooling and pressurizing the liquid gas.
In each of the above embodiments, the temperature varying device 2 includes a heat exchanger mechanism having a low-pressure circuit and a high-pressure circuit, and a second blower 8, an inlet end 8a of the second blower 8 is communicated with the low-pressure circuit of the heat exchanger mechanism, and an outlet end 8b of the second blower 8 is communicated with the high-pressure circuit of the heat exchanger mechanism.
In one embodiment, the heat exchange mechanism includes a recuperative heat exchanger 4, a first heat exchanger 3, and a second heat exchanger 7, the recuperative heat exchanger 4, the second heat exchanger 7, and a second blower 8 are sequentially connected in series, and the first heat exchanger 3 is connected in parallel with the second heat exchanger 7.
In one embodiment, the temperature varying device 2 further comprises a temperature regulating valve 9, which is configured in the high-pressure loop of the temperature varying device and is used for controlling the flow distribution of the high-temperature high-pressure steam output by the blower between the first heat exchanger and the second heat exchanger, so as to control the temperature range of the high-temperature steam output by the first heat exchanger.
In one embodiment, the heat exchange mechanism further comprises a third heat exchanger 71, the third heat exchanger 71 being adapted to increase the temperature difference between the high-pressure circuit and the low-pressure circuit at the high temperature end of the second heat exchanger 7.
Preferably, the second blower 8 and/or the first heat exchanger 3 and/or the second heat exchanger 7 and/or the third heat exchanger 71 are provided with insulation.
In addition to the temperature changing device 2, other members having a large difference from the ambient temperature also have insulating layers.
In the above embodiments, the gas liquefaction path is constituted by the first blower 14, the gas filter 13, the gas cooler 12, the flash tank 17, the condenser-evaporator 1, the nitrogen compressor 16, and the liquid gas pressurizing pump 15, and the gas is supplied to pressurize, filtered, cooled, liquefied, flash separated, cooled, and then discharged.
The zero-carbon power generation device composed of the temperature changing device 2 and the Rankine cycle of the cold power generator 11 absorbs the heat of the gas by utilizing the refrigeration function of the gas liquefaction passage and converts the heat into electric energy and heat energy, and specifically comprises the following steps:
the first blower 14 pressurizes the gas, so that the gas can flow by overcoming the on-way resistance, the gas filter 13 separates dust particles, volatile gas, moisture and carbon dioxide in the gas, the cleanliness of air separation gas is guaranteed, frosting in the cooling process is prevented, and meanwhile, moisture collection and carbon dioxide capture can be realized; the low-temperature inlet end of the gas cooler 12 flows through low-temperature liquid (system working medium) at minus 195 ℃ in Rankine cycle to cool the gas entering from the high-temperature inlet end of the gas cooler 12 to be close to minus 195 ℃, and the gas is liquefied; the gas pressure is reduced due to the pumping action of the nitrogen compressor in the flash tank 17, the liquid oxygen is still kept in a liquid state due to the fact that the critical temperature is 183 ℃ higher, the liquid nitrogen is converted into gas (nitrogen is separated from the gas) from the liquid due to the pressure reduction, the nitrogen compressor 16 pressurizes the nitrogen, the nitrogen is sent into the condenser-evaporator 1 to be cooled again, the liquid nitrogen is output outwards finally, the liquid gas enters from the middle upper portion of the flash tank 17, gas containing oxygen and argon can be obtained at the bottom of the flash tank 17, the liquid oxygen containing the liquid argon can be directly output through the liquid gas pressurizing pump 15, and the flash, cooling and pressurizing can be carried out again to enter a part of the liquid oxygen and the liquid argon to be separated.
The Rankine cycle system of the gas liquefaction passage, the temperature changing device 2 and the cold power generator 11 forms a zero-carbon gas liquefaction power generation device, and specifically:
the Rankine cycle of the cold power generator 11 is formed by five parts of a liquid pressurizing pump 10, a gas cooler 12, a first heat exchanger 3, the cold power generator 11 and the condenser-evaporator 1; the gas cooler 12 receives the energy of the gas cooling liquefaction passage and is an energy input end of a low-temperature region of a Rankine cycle high-pressure loop; after the temperature changing device 2 lifts low-temperature exhaust steam discharged by the cold power generator into high-temperature steam, the first heat exchanger 3 transfers the energy of the high-temperature exhaust steam to a high-temperature region of a Rankine cycle high-pressure loop of the cold power generator 11, the heat energy of gas input from the outside of the low-temperature region of the high-pressure loop and the heat energy of high temperature returned by the exhaust gas of the high-temperature region of the high-pressure loop jointly form an energy source of Rankine cycle, only the energy input from the outside is the output energy of the temperature changing device 2 and the cold power generator 11, and the energy for lifting the exhaust gas is only repeatedly circulated in the cold power generation system to do useless work, but the energy is indispensable, and the gas heat energy can be perfectly converted into electric energy only by the energy source.
The temperature changing device 2 improves the low-temperature energy into high-temperature energy: the external gas enters the gas cooler 12 to exchange heat with the liquid working medium, the gas is cooled, the temperature of the liquid working medium is raised, and the enthalpy value is increased; the exhaust gas of the cold power generator 11 enters the condenser-evaporator 1 to exchange heat with the liquid working medium, the exhaust gas is condensed into liquid, and the energy in the exhaust gas is converted into low-temperature steam to manufacture a low-temperature cold source; the temperature changing device 2 is composed of a heat exchange mechanism with a high-pressure loop and a low-pressure loop and a second blower 8 which are connected in series, under the pumping action of the second blower 8, low-temperature steam enters from a low-pressure loop of the heat exchange mechanism, is pressurized and heated by the second blower 8 and then returns to a high-pressure loop of the heat exchange mechanism, the temperature difference occurs in the high-low pressure loop in the heat exchange mechanism, so that the high-pressure loop heats the low-pressure loop, the constant-pressure enthalpy increase of the low-pressure loop and the constant-pressure enthalpy drop of the high-pressure loop are realized, the high-temperature steam is continuously cooled and finally becomes liquid to return to the condenser-evaporator 1, the heat exchange mechanism is repeatedly circulated, so that the temperature of the gas in the inlet loop of the second blower 8 is greatly increased, the temperature of the inlet steam can be greatly increased as required only by compressing the second blower 8 by small potential energy, and the function of a self-feedback hot compressed steam temperature rising device is realized; sending the high-temperature steam with the increased temperature to a first heat exchanger 3 connected with a Rankine cycle for heat exchange, after cooling and temperature reduction, returning the high-temperature steam of the first heat exchanger 3 to the low-temperature end of a second heat exchanger 7, continuously condensing the high-temperature steam into liquid, and returning the liquid to the condenser-evaporator 1; the second heat exchanger 7 of the rankine cycle obtains energy, and the high-pressure liquid is changed into high-temperature high-pressure steam to provide energy for the operation of the cold power generator 11; the condenser-evaporator 1 is provided with a low-temperature cold source, so that the condensing temperature of the dead steam of the cold power generator 11 is not influenced by the ambient temperature, the temperature of a nitrogen system can be reduced to 196 ℃ below zero, and conditions are created for the operation of the cryogenic cold power generator 11; the high-temperature steam after the temperature of the exhaust gas heat energy is increased by the first heat exchanger 3 of the temperature changing device 2 is transferred to the cold power generator 11 of the Rankine cycle, so that a high-temperature heat source is provided for the Rankine cycle, and the aim of converting the gas heat energy into the electric energy by the Rankine cycle is fulfilled without any fossil energy. The critical temperature of the air is-190 ℃ at 0.16 MPa, nitrogen is used as a system working medium of the Rankine cycle and temperature changing device 2, the critical temperature of the nitrogen is-196 ℃ at 0.1 MPa and is lower than the critical temperature of the air at 0.16 MPa, and conditions are created for liquefying the gas. The temperature changing device 2 raises the exhaust gas energy and the air heat energy of the system from low temperature to high temperature, the consumed power is only about 5% of the latent heat power of the working medium, the energy consumed by the temperature changing device 2 is mainly used for dragging the second air blower 8, the second air blower 8 can be dragged by an independent motor or a small-sized cold turbine, and the energy consumed by the second air blower 8 during working is converted into the heat of the temperature changing device 2 and returns to a high-temperature high-pressure loop of the cold turbine, so that the second air blower 8 essentially does not consume energy.
The full necessary condition of the Rankine cycle of the cold power generator 11 is that a low-temperature cold source and a high-temperature heat source are provided, the condenser-evaporator 1 has a refrigeration function, heat energy contained in returned liquid and exhaust gas of the cold power generator are regarded as external energy sources to be evaporated, liquid working media are changed into low-temperature steam, and the effect brought by the low-temperature cold source, namely the condensation of the exhaust gas, is realized; the first heat exchanger 3 transfers the environmental energy collected and promoted by the temperature changing device 2 to the high-pressure loop of the cold power generator 11, so as to provide a high-temperature heat source for the operation of the cold power generator 11.
According to the connection relation and the principle of the embodiment, the method is specifically designed and assembled, and parameters are set and tested:
a zero-carbon air liquefaction power generation device with 100000NM/H oxygen yield has the density of 1.43g/L of oxygen under standard conditions, the mass of 100000NM/H oxygen is 143 tons, the volume of air is 1L, oxygen accounts for 0.21L of the volume of air because the volume fraction of oxygen in air is 21%, the mass of air is 1L multiplied by 1.293g/L is 1.293g, the mass of oxygen is 0.21L multiplied by 1.429g/L is 0.3g, the mass fraction of oxygen in air is 0.3g, 0.3/1.293g multiplied by 100% 23.2% of oxygen accounts for 23.2% of the proportion of air, the total amount of air to be liquefied is 143 divided by 0.232 to 616 tons, the physical property table of air is inquired, the entropy of air is compressed to 0.16 MPa, the energy consumption is 43kj/kg, the temperature is increased from 20 degrees to 62 degrees, the temperature of air is increased to 62 degrees under zero degrees, the temperature is 62 degrees under zero degrees and the temperature is cooled to 62 degrees, the heat required to be transferred is 454 kilowatts, and the heat required to be transferred by 616 tons of air is total:
the electricity consumption 616 × 1000 × 43 × 1.1/3600 ═ 8093kw in the blower and the like is subtracted from 616 × 1000 × 454/3600 ═ 77684kw, and the electricity quantity that can be output to the outside is: 77684 8093 (69591 kw).
In the existing technology, the electric energy required by each ton of oxygen production is 660 degrees, and the electric energy required by the 143 tons of oxygen production is as follows: 143 × 660 — 94380kw, decreasing the payout equals increasing the revenue, and the total benefit after adding the two is: 94380+69591 is 163971Kw, calculated by current commercial electricity price of 0.72 yuan/degree in Jiangsu province, the benefit generated per hour is 163971 × 0.72 is 118059 yuan, and 118059 × 8000 is 944472960 yuan calculated by 8000 hours all the year.
After an air separation enterprise producing 110 ten thousand tons of oxygen annually adopts a zero-carbon air liquefaction power generation device, the benefit of annual energy conservation reaches 9 hundred million and more, which is enough to swing the root of the whole industry.
The Rankine cycle adopts nitrogen as a working medium, parameters of an air inlet end of a cold power generator 11 are that steam pressure is 10 MPa, temperature is 55 ℃ below zero, and a corresponding enthalpy value is 186 kj/kg; the parameters of the exhaust end of the cold power generator 11 are that the exhaust pressure is 0.1 MPa, the temperature is-196 ℃, the enthalpy value is 84kj/kg., the theoretical enthalpy drop of a unit working medium of the cold power generator 11 is 186-84 kj/kg, and under the current technical level, the isentropic efficiency of the cold power generator 11 can only be 0.88, so that the actual enthalpy drop of the cold power generator 11 is 0.88-89.76 kj/kg, the increased 8kj/kg when the liquid pressurizing pump 10 pressurizes the liquid with 0.1 MPa to the pressure with 10 MPa is reduced, and finally the net enthalpy drop of the cold power generator 11 is only 89.76-8-81.76 kj/kg; the energy transmitted to the Rankine cycle of the cold power generator 11 by the air liquefaction system is 77684kw, so that the working medium flow rate of the corresponding Rankine cycle in unit time is 77684/81.76 which is 950 kg; the temperature of the low-pressure inlet end of the liquid pressure pump 10 is-196 ℃, the enthalpy value is-122 kj/kg, the pressure is 0.1 MPa, after the liquid pressure pump 10 is pressurized, the enthalpy value of the high-pressure outlet end of the liquid pressure pump 10 is increased to-114 kj/kg, the pressure is increased to 10 MPa, the temperature is increased to-195 ℃, after the liquid pressure pump is heated by the air cooler 18, the pressure of the high-temperature outlet end of the air cooler is equal to 10 MPa, the enthalpy value is increased to-32.24 kj/kg, and the temperature is increased to-155 ℃; the total enthalpy value from the high-pressure inlet end of the cold power generator 11 to the low-pressure inlet end of the liquid pressurizing pump 10 is 186+ 122-308 kj/kg, wherein only 89.76kj/kg is converted into electric energy, so that the generating efficiency of the Rankine cycle is only 89.76 ÷ 308-0.2914, and nearly 71% of exhaust gas energy is repeatedly circulated in the Rankine cycle to do useless work; the full efficiency of the cold-power generator 11, calculated as the net enthalpy drop of the cold-power generator 11, is only 81.76 ÷ 308 ÷ 0.2654, less the energy consumed by the liquid-pressurizing pump 10.
The temperature changing device 2 and the condensation-evaporator 1 complete the function of a condenser in the common Rankine cycle under the condition of no low-temperature cold source, so that an air heat energy generator is realized; the-196 ℃ low-temperature air generated when the liquid nitrogen in the condenser-evaporator 1 is evaporated is utilized, the temperature difference is utilized, the heat in the air is continuously received as the energy source of the cold power generator 11, and the air is gradually changed into liquid due to the continuous transfer of the energy in the air, and the electric energy generated by receiving the energy from the air has a large amount of surplus besides the energy required by the blower and can be transmitted to the outside, so the device is called as a zero-carbon gas liquefaction power generation device.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
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| CN114248629A (en) * | 2021-09-18 | 2022-03-29 | 成都佳灵绿色能源有限责任公司 | Automobile air energy generator and method for driving automobile |
| WO2023040192A1 (en) * | 2021-09-18 | 2023-03-23 | 成都佳灵绿色能源有限责任公司 | Temperature-changing device and system, and method for increasing temperature of low-temperature steam |
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