CN207751221U - A kind of heat pump air-seperation system of LNG cold energy uses - Google Patents
A kind of heat pump air-seperation system of LNG cold energy uses Download PDFInfo
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- CN207751221U CN207751221U CN201820020393.6U CN201820020393U CN207751221U CN 207751221 U CN207751221 U CN 207751221U CN 201820020393 U CN201820020393 U CN 201820020393U CN 207751221 U CN207751221 U CN 207751221U
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 255
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 127
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 238000000926 separation method Methods 0.000 claims abstract description 50
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 21
- 239000002699 waste material Substances 0.000 claims description 25
- 238000009833 condensation Methods 0.000 claims description 19
- 230000005494 condensation Effects 0.000 claims description 19
- 239000002808 molecular sieve Substances 0.000 claims description 18
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 18
- 238000003860 storage Methods 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 abstract description 12
- 230000006835 compression Effects 0.000 abstract description 4
- 238000007906 compression Methods 0.000 abstract description 4
- OLBVUFHMDRJKTK-UHFFFAOYSA-N [N].[O] Chemical compound [N].[O] OLBVUFHMDRJKTK-UHFFFAOYSA-N 0.000 abstract description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 2
- 206010021703 Indifference Diseases 0.000 abstract 1
- 238000004821 distillation Methods 0.000 abstract 1
- 239000003570 air Substances 0.000 description 116
- 239000003949 liquefied natural gas Substances 0.000 description 41
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 238000000034 method Methods 0.000 description 8
- 238000010992 reflux Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 239000012535 impurity Substances 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- -1 moisture Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a kind of heat pump air-seperation systems of LNG cold energy uses, raw material low-pressure air is cooled down using LNG cold energy, and air separation is carried out in the way of heat pump distillation, compared to traditional space division system, the utility model is only pressurized to 0.56MPa or so using heat pump rectification system to the part nitrogen in raw air, reduces the total wasted work of compression member in space division system；Using LNG, cooling raw air, part cold energy can be changed into the work of separation of oxygen nitrogen in main heat exchanger, and liquid oxygen product needs not move through main heat exchanger heat absorption and releases cold, and liquid device processed can save；Utility model cools down raw air using LNG, and space division system can also be greatly lowered and start the time；Due to pressure reduction, rectifying column cost of equipment is greatly lowered compared to traditional space division system, and using the investment of nitrogen booster arrangement also below original air compressor system, stripping tower and traditional space division system and indifference, therefore system gross investment can reduce.
Description
Technical Field
The utility model belongs to the air separation field relates to a heat pump air separation system, especially relates to a heat pump air separation system that LNG cold energy utilized.
Background
Air separation systems are important in the steel, chemical, semiconductor, food processing and medical fields. The cryogenic rectification air separation system is realized in a large scaleThe main scheme for preparing high-purity nitrogen, oxygen and argon in a large scale. The cryogenic rectification air separation system consumes a large amount of energy, especially in the production process of liquid oxygen and liquid nitrogen. Liquefied Natural Gas (LNG) is a low-temperature (about 111K) mixed liquid obtained by liquefying natural gas by a cryogenic process, and the main component of the liquefied natural gas is methane (CH)4) The method has the advantages of high combustion heat value, low emission pollution, low storage and transportation cost and the like. LNG cold energy is huge in quantity and high in energy level, and common applications mainly comprise direct power generation, air liquefaction and separation, liquefied dry ice preparation, cryogenic grinding, a low-temperature refrigeration house and the like. Considering that the process temperature of the air separation system is about 78-100K and is lower than the temperature of LNG, the condition of low-temperature cold energy and high-temperature use can be avoided, and the efficient utilization principle of temperature-to-opening and gradient utilization energy is met, so the cold energy utilization scheme is considered to be the most reasonable utilization mode in the prior art.
The energy-saving effect of the existing LNG cold energy utilization air separation system can be mainly divided into the following two factors: (1) the LNG cold energy cools the temperature of the working medium at the inlet of the air compressor or the nitrogen compressor, so that the demand of an air separation system on electric power energy consumption is reduced; (2) the LNG cold energy can replace the high-purity liquid oxygen/liquid nitrogen cold release amount entering the main heat exchanger to realize the reduction of the temperature of the raw material air, and the additional electric energy consumption required for preparing the cold energy of the low-temperature liquid product is reduced. Through relevant literature and patent calculation, compared with a conventional air separation system, the energy consumption of preparing unit liquid products by adopting the air separation system with LNG cold energy can be reduced by about 50%.
However, the operating pressure of the rectifying tower of the existing air separation system scheme utilizing the LNG cold energy is close to 0.6MPa, and the addition of the cold energy only reduces the energy consumption for producing liquid products and has no beneficial effect on the separation work of the air separation system. There are 2 main reasons for this phenomenon: (1) the rectification unit of the traditional air separation system adopts a double-stage rectification tower, the reflux gas-liquid of an upper tower and a lower tower is realized through the heat exchange of low-pressure liquid oxygen and high-pressure nitrogen, and the boiling point of the nitrogen is far lower than that of oxygen under the same pressure, so that the lower rectification tower needs to operate at high pressure; (2) the working temperature of the double-stage rectifying tower is 78-100K, the storage temperature of LNG is 112K, if LNG cold energy acts on the rectifying process, the raw material air still needs to be pressurized, and lower working temperature is generated through expansion or throttling. The method for adjusting the two reasons only reduces the pressure of the rectifying tower by changing the traditional double-stage rectifying cold-heat coupling mode, converts part of LNG cold energy into separation work, and further reduces the energy consumption of the air separation system for utilizing the LNG cold energy.
SUMMERY OF THE UTILITY MODEL
The shortcoming and the not enough to prior art, the utility model aims at providing a heat pump air separation system that LNG cold energy utilized, adopts LNG cold energy cooling raw materials low-pressure air to utilize heat pump rectification mode to carry out air separation, thereby reduce the total power consumption of compression part among the air separation system, reduce air separation system start-up time, reduce the total investment cost of system.
The utility model discloses a solve the technical scheme that its technical problem adopted and do:
a heat pump air separation system utilizing LNG cold energy comprises an air compressor, a water cooling tower, a molecular sieve, a main heat exchanger, a subcooler I, a rectifying tower, a subcooler II, a stripping tower, a supercharger, a condensing evaporator, an LNG storage device, a cryogenic pump and a liquid oxygen storage device,
the main heat exchanger comprises an air passage, an LNG passage, a nitrogen passage and a waste nitrogen passage; the subcooler I comprises an air passage, a nitrogen passage I, a waste nitrogen passage and a nitrogen passage II; the rectifying tower is provided with tower plates in the height direction in a staggered manner, the bottom of the rectifying tower is provided with an air inlet and a liquid air outlet, and the top of the rectifying tower is provided with a liquid nitrogen inlet and a nitrogen outlet; the subcooler II comprises a liquid air passage, a nitrogen passage, a waste nitrogen passage and a liquid nitrogen passage; the stripping tower is provided with tower plates in the height direction in a staggered way, the bottom of the stripping tower is provided with a liquid oxygen outlet I, a liquid oxygen outlet II and a liquid oxygen inlet, the upper part of the stripping tower is provided with a liquid air inlet, a liquid nitrogen inlet, a pure nitrogen outlet and a waste nitrogen outlet, wherein,
an outlet of the LNG storage device is communicated with an LNG passage of the main heat exchanger through a pipeline and the cryogenic pump; an air inlet of the air compressor is communicated with the outside air, and an air outlet of the air compressor is communicated with an air inlet at the bottom of the rectifying tower through pipelines sequentially passing through the water cooling tower, the molecular sieve, an air passage of the main heat exchanger and an air passage of the subcooler I; a liquid air outlet at the bottom of the rectifying tower is communicated with a liquid air inlet at the upper part of the stripping tower through a liquid air passage of the subcooler II through a pipeline, and a nitrogen outlet at the top of the rectifying tower is communicated with a liquid nitrogen side inlet of the condensation evaporator through a nitrogen passage II of the supercharger and the subcooler I in sequence through pipelines; the liquid nitrogen side outlet of the condensation evaporator is divided into two paths, one path is communicated with the liquid nitrogen inlet at the top of the rectifying tower, and the other path is communicated with the liquid nitrogen inlet at the upper part of the stripping tower through the liquid nitrogen passage of the subcooler II; a liquid oxygen side inlet of the condensation evaporator is communicated with a liquid oxygen outlet I at the bottom of the stripping tower, and a liquid oxygen side outlet of the condensation evaporator is communicated with a liquid oxygen inlet at the bottom of the stripping tower; a liquid oxygen outlet II at the bottom of the stripping tower is communicated with an inlet of the liquid oxygen storage device through a pipeline; and a pure nitrogen outlet at the upper part of the stripping tower sequentially passes through the nitrogen passage of the subcooler II, the nitrogen passage I of the subcooler I and the inlet of the nitrogen passage of the main heat exchanger through pipelines, and a waste nitrogen outlet at the upper part of the stripping tower sequentially passes through the waste nitrogen passage of the subcooler II, the waste nitrogen passage of the subcooler I and the inlet of the waste nitrogen passage of the main heat exchanger through pipelines.
Preferably, the outlet of the nitrogen passage of the main heat exchanger is in communication with the inlet of a nitrogen storage or utilization device.
Preferably, the outlet of the dirty nitrogen passage of the main heat exchanger is in communication with an air cooling system of the molecular sieve.
Preferably, a control valve is arranged at a liquid nitrogen inlet at the top of the rectifying tower.
Preferably, the liquid air inlet and the liquid nitrogen inlet at the upper part of the stripping tower are both provided with control valves.
Preferably, the outlet pressure of the air compressor is about 0.2 MPa.
Preferably, the high-purity nitrogen gas led out from the top of the rectifying tower is pressurized to about 0.56MPa by the booster.
The utility model discloses a heat pump air separation system that LNG cold energy utilized mainly adopts LNG cold energy cooling raw materials low-pressure air to utilize heat pump rectification mode to carry out air separation, its concrete working process is:
the method comprises the following steps that air is firstly boosted to 0.2MPa by an air compressor and cooled by a water cooling tower, the boosted pressure is used for compensating the pressure loss in a molecular sieve, a main heat exchanger, a subcooler I, a rectifying tower and a stripping tower, and the air cooled by the water cooling tower enters the molecular sieve to remove impurities such as moisture, carbon dioxide and the like; the pressurized normal temperature air purified by the molecular sieve enters a main heat exchanger and is cooled to the temperature close to the bubble point by LNG, reflux nitrogen and polluted nitrogen, the pressurized normal temperature air is sent to the bottom of a rectifying tower, rising air and reflux liquid nitrogen injected from the top are repeatedly condensed and evaporated on tower plates which are arranged in a staggered mode in the height direction in the rectifying tower, oxygen-enriched liquid air with higher oxygen concentration is concentrated at the bottom of the rectifying tower, and high-purity nitrogen is concentrated at the top of the rectifying tower; oxygen-enriched liquid air extracted from the bottom of the rectifying tower passes through a cooler II and then enters the upper part of the stripping tower to carry out oxygen stripping; the high-purity nitrogen led out from the upper part of the rectifying tower is pressurized to about 0.56MPa by a supercharger, then is cooled by a cooler I, then enters a condensation evaporator for condensation, returns to the top parts of the rectifying tower and the stripping tower as reflux liquid, and liquid oxygen generated at the bottom part of the stripping tower absorbs heat in the condensation evaporator for evaporation and returns to the stripping tower; liquid oxygen at the bottom of the stripping tower is directly output as a product, pure nitrogen at the top of the stripping tower is output as a nitrogen product after being reheated by the cooler II and the main heat exchanger, and dirty nitrogen is sent to the molecular sieve purification system and the air cooling system after being reheated by the cooler II and the main heat exchanger.
Compared with the prior art, the utility model discloses a heat pump air separation system that LNG cold energy utilized has apparent technological effect: (1) compared with the traditional air separation system, the utility model adopts the heat pump rectification system to pressurize partial nitrogen in the raw air to about 0.56MPa, thereby reducing the total power consumption of the compression part in the air separation system; (2) LNG is adopted to cool raw material air in the main heat exchanger, part of cold energy can be converted into oxygen-nitrogen separation power, liquid oxygen products do not need to absorb heat and release cold through the main heat exchanger, and a liquid preparation device can be omitted; (3) the utility model adopts LNG to cool the raw material air, which can greatly reduce the starting time of the air separation system; (4) the utility model discloses in, because pressure reduction, rectifying column equipment expense is compared and is reduced in traditional air separation system by a wide margin, adopts nitrogen booster equipment investment also to be less than original air compressor machine system, and the stripping column does not have the difference with traditional air separation system, therefore the total investment of system can reduce.
Drawings
Fig. 1 is the schematic diagram of the heat pump air separation system for LNG cold energy utilization of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention will be further described in detail with reference to the accompanying drawings and examples. It should be noted that the following description is only a preferred embodiment of the present invention, and does not limit the scope of the present invention.
As shown in fig. 1, the utility model discloses a heat pump air separation system that LNG cold energy utilized, including air compressor machine 1, water cooling tower 2, molecular sieve 3, main heat exchanger 4, subcooler I5, rectifying column 6, subcooler II 7, stripping column 8, booster 9, condensation evaporator 10, LNG storage device 11, cryopump 12, liquid oxygen storage device 13. The main heat exchanger 4 comprises an air passage, an LNG passage, a nitrogen passage and a waste nitrogen passage; the subcooler I5 comprises an air passage, a nitrogen passage I, a waste nitrogen passage and a nitrogen passage II; the rectifying tower 6 is provided with tower plates in the height direction in a staggered manner, the bottom of the rectifying tower is provided with an air inlet and a liquid air outlet, and the top of the rectifying tower is provided with a liquid nitrogen inlet and a nitrogen outlet; the subcooler II 7 comprises a liquid air passage, a nitrogen passage, a waste nitrogen passage and a liquid nitrogen passage; the stripping tower 8 is provided with tower plates arranged in the height direction in a staggered manner, the bottom of the stripping tower is provided with a liquid oxygen outlet I, a liquid oxygen outlet II and a liquid oxygen inlet, and the upper part of the stripping tower is provided with a liquid air inlet, a liquid nitrogen inlet, a pure nitrogen outlet and a waste nitrogen outlet.
The outlet of the LNG storage 11 is connected to the LNG passage of the main heat exchanger 4 via a cryogenic pump 12 via a pipeline. An air inlet of an air compressor 1 is communicated with air, and an air outlet of the air compressor 1 is communicated with an air inlet at the bottom of a rectifying tower 6 through pipelines sequentially passing through an air passage of a water cooling tower 2, a molecular sieve 3 and a main heat exchanger 4 and an air passage of a subcooler I5; a liquid air outlet at the bottom of the rectifying tower 6 is communicated with a liquid air inlet arranged at the upper part of the stripping tower 8 through a liquid air passage of a cooler II 7 by a pipeline, a nitrogen outlet at the top of the rectifying tower 6 is communicated with a liquid nitrogen side inlet of the condensation evaporator 10 through a nitrogen passage II of a supercharger 9 and a subcooler I5 in sequence by pipelines, the liquid nitrogen side outlet of the condensation evaporator 10 is divided into two paths, one path is communicated with the liquid nitrogen inlet at the top of the rectifying tower 6, and the other path is communicated with the liquid nitrogen inlet at the upper part of the stripping tower 8 through a liquid nitrogen passage of the cooler II 7; a liquid oxygen side inlet of the condensation evaporator 10 is communicated with a liquid oxygen outlet I at the bottom of the stripping tower 8, and a liquid oxygen side outlet of the condensation evaporator 10 is communicated with a liquid oxygen inlet at the bottom of the stripping tower 8; a liquid oxygen outlet II at the bottom of the stripping tower 8 is communicated with an inlet of a liquid oxygen storage device 13 through a pipeline; the pure nitrogen outlet at the upper part of the stripping tower 8 is communicated with the inlet of a nitrogen storage device (not shown in the figure) through a nitrogen passage of the cooler II 7, a nitrogen passage I of the subcooler I5 and a nitrogen passage of the main heat exchanger 4 in sequence through pipelines, and the waste nitrogen outlet at the upper part of the stripping tower 8 is communicated with the air cooling system of the molecular sieve 3 through a waste nitrogen passage of the cooler II 7, a waste nitrogen passage of the subcooler I5 and a waste nitrogen passage of the main heat exchanger 4 in sequence through pipelines.
The utility model discloses a heat pump air separation system that LNG cold energy utilized mainly adopts LNG cold energy cooling raw materials low-pressure air to utilize heat pump rectification mode to carry out air separation, its concrete working process is:
the air is firstly boosted to 0.2MPa by an air compressor 1 and cooled by a water cooling tower 2, the boosted pressure is used for compensating the pressure loss in a molecular sieve 3, a main heat exchanger 4, a subcooler I5, a rectifying tower 6 and a stripping tower 7, and the air cooled by the water cooling tower 2 enters the molecular sieve 3 to remove impurities such as moisture, carbon dioxide and the like in the air; the pressurized normal temperature air purified by the molecular sieve 3 enters the main heat exchanger 4 and is cooled to the temperature close to the bubble point by LNG, reflux nitrogen and polluted nitrogen, and then the air is sent to the bottom of the rectifying tower 5, the rising air and reflux liquid nitrogen injected from the top are repeatedly condensed and evaporated by tower plates arranged in the rectifying tower 6 in a staggered manner in the height direction, so that oxygen-enriched liquid air with higher oxygen concentration is concentrated at the bottom of the rectifying tower 6, and high-purity nitrogen is concentrated at the top of the rectifying tower 6; oxygen-enriched liquid air extracted from the bottom of the rectifying tower 6 passes through a cooler II 7 and then enters the upper part of a stripping tower 8 to carry out oxygen stripping; high-purity nitrogen led out from the upper part of the rectifying tower 6 is pressurized to about 0.56MPa by a supercharger 9, then is cooled by a cooler I5, then enters a condensation evaporator 10 for condensation, returns to the tops of the rectifying tower 5 and the stripping tower 8 as reflux, and liquid oxygen generated at the bottom of the stripping tower 8 absorbs heat in the condensation evaporator 10 for evaporation and returns to the stripping tower 8; and part of liquid oxygen at the bottom of the stripping tower 8 is directly output as a product, pure nitrogen at the top of the stripping tower 8 is output as a nitrogen product after being reheated by the cooler II 7 and the main heat exchanger 4, and dirty nitrogen is sent to the molecular sieve 3 purification system and the air cooling system after being reheated by the cooler II 7 and the main heat exchanger 4.
Furthermore, a liquid nitrogen inlet at the top of the rectifying tower 6 is provided with a control valve, and a liquid air inlet and a liquid nitrogen inlet at the upper part of the stripping tower 8 are both provided with control valves.
Compared with the traditional air separation system, the utility model adopts the heat pump rectification system to pressurize partial nitrogen in the raw air to about 0.56MPa, thereby reducing the total power consumption of the compression part in the air separation system; the raw material air is pre-pressurized by an air compressor 1 and then enters a molecular sieve 3 for impurity removal, so that the problem of icing generated by heat exchange of the raw material air, LNG, nitrogen and waste nitrogen in a main heat exchanger 4 can be solved; adopt LNG cooling raw materials air in main heat exchanger 4, partial cold energy can be changeed into the work of separation of oxygen nitrogen, and liquid oxygen product need not through the heat absorption of main heat exchanger and releases cold, and the system liquid device can save, simultaneously the utility model discloses a LNG cooling raw materials air can reduce air separation system start-up time by a wide margin, because pressure reduces, and rectifying column equipment cost compares and reduces by a wide margin in traditional air separation system, adopts nitrogen booster equipment investment also to be less than original air compressor machine system, and the stripping column does not have the difference with traditional air separation system, therefore the total investment of system can reduce.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (5)
1. A heat pump air separation system utilizing LNG cold energy comprises an air compressor, a water cooling tower, a molecular sieve, a main heat exchanger, a subcooler I, a rectifying tower, a subcooler II, a stripping tower, a supercharger, a condensing evaporator, an LNG storage device, a cryogenic pump and a liquid oxygen storage device,
the main heat exchanger comprises an air passage, an LNG passage, a nitrogen passage and a waste nitrogen passage;
the subcooler I comprises an air passage, a nitrogen passage I, a waste nitrogen passage and a nitrogen passage II;
the rectifying tower is provided with tower plates in the height direction in a staggered manner, the bottom of the rectifying tower is provided with an air inlet and a liquid air outlet, and the top of the rectifying tower is provided with a liquid nitrogen inlet and a nitrogen outlet;
the subcooler II comprises a liquid air passage, a nitrogen passage, a waste nitrogen passage and a liquid nitrogen passage;
the stripping tower is provided with tower plates in the height direction in a staggered way, the bottom of the stripping tower is provided with a liquid oxygen outlet I, a liquid oxygen outlet II and a liquid oxygen inlet, the upper part of the stripping tower is provided with a liquid air inlet, a liquid nitrogen inlet, a pure nitrogen outlet and a waste nitrogen outlet,
wherein,
an outlet of the LNG storage device is communicated with an LNG passage of the main heat exchanger through a pipeline and the cryogenic pump;
an air inlet of the air compressor is communicated with the outside air, and an air outlet of the air compressor is communicated with an air inlet at the bottom of the rectifying tower through pipelines sequentially passing through the water cooling tower, the molecular sieve, an air passage of the main heat exchanger and an air passage of the subcooler I;
a liquid air outlet at the bottom of the rectifying tower is communicated with a liquid air inlet at the upper part of the stripping tower through a liquid air passage of the subcooler II through a pipeline, and a nitrogen outlet at the top of the rectifying tower is communicated with a liquid nitrogen side inlet of the condensation evaporator through a nitrogen passage II of the supercharger and the subcooler I in sequence through pipelines;
the liquid nitrogen side outlet of the condensation evaporator is divided into two paths, one path is communicated with the liquid nitrogen inlet at the top of the rectifying tower, and the other path is communicated with the liquid nitrogen inlet at the upper part of the stripping tower through the liquid nitrogen passage of the subcooler II; a liquid oxygen side inlet of the condensation evaporator is communicated with a liquid oxygen outlet I at the bottom of the stripping tower, and a liquid oxygen side outlet of the condensation evaporator is communicated with a liquid oxygen inlet at the bottom of the stripping tower; a liquid oxygen outlet II at the bottom of the stripping tower is communicated with an inlet of the liquid oxygen storage device through a pipeline;
and a pure nitrogen outlet at the upper part of the stripping tower sequentially passes through the nitrogen passage of the subcooler II, the nitrogen passage I of the subcooler I and the inlet of the nitrogen passage of the main heat exchanger through pipelines, and a waste nitrogen outlet at the upper part of the stripping tower sequentially passes through the waste nitrogen passage of the subcooler II, the waste nitrogen passage of the subcooler I and the inlet of the waste nitrogen passage of the main heat exchanger through pipelines.
2. An LNG cold energy utilizing heat pump air separation system according to claim 1, characterized in that the outlet of the nitrogen passage of the main heat exchanger is in communication with the inlet of a nitrogen storage or utilizing device.
3. The LNG cold energy utilization heat pump air separation system of claim 1, wherein an outlet of the dirty nitrogen path of the primary heat exchanger is in communication with an air cooling system of the molecular sieve.
4. The LNG cold energy utilization heat pump air separation system of claim 1, wherein a control valve is arranged at a liquid nitrogen inlet at the top of the rectifying tower.
5. The LNG cold energy utilization heat pump air separation system of claim 1, wherein control valves are arranged at a liquid air inlet and a liquid nitrogen inlet of the upper part of the stripping tower.
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| CN201820020393.6U CN207751221U (en) | 2018-01-07 | 2018-01-07 | A kind of heat pump air-seperation system of LNG cold energy uses |
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| CN201820020393.6U CN207751221U (en) | 2018-01-07 | 2018-01-07 | A kind of heat pump air-seperation system of LNG cold energy uses |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108036585A (en) * | 2018-01-07 | 2018-05-15 | 中国科学院工程热物理研究所 | A kind of heat pump air-seperation system of LNG cold energy uses |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108036585A (en) * | 2018-01-07 | 2018-05-15 | 中国科学院工程热物理研究所 | A kind of heat pump air-seperation system of LNG cold energy uses |
| CN108036585B (en) * | 2018-01-07 | 2024-03-05 | 中国科学院工程热物理研究所 | Heat pump air separation system for LNG cold energy utilization |
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