CN216522650U - Liquid oxygen liquefaction air separation plant - Google Patents
Liquid oxygen liquefaction air separation plant Download PDFInfo
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- CN216522650U CN216522650U CN202123098765.8U CN202123098765U CN216522650U CN 216522650 U CN216522650 U CN 216522650U CN 202123098765 U CN202123098765 U CN 202123098765U CN 216522650 U CN216522650 U CN 216522650U
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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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
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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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
- F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion 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
- 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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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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
The utility model discloses a liquid oxygen liquefaction air separation device, which directly enters a medium-pressure tower for rectification without arranging a gas-liquid separator and a throttle valve behind a main heat exchanger, improves the operating pressure of a low-pressure tower as much as possible under the condition of ensuring heat exchange temperature difference, utilizes the pressure of return gas in the low-pressure tower to add a gas expander, has high refrigeration efficiency compared with the throttle valve, and reduces the energy consumption of the device; the novel rectifying tower adopts a newly added backflow gas expander to replace a medium-pressure air throttle valve, improves the refrigeration efficiency, reduces the energy consumption of the device, fully utilizes the tower loading pressure by improving the operating pressure of the rectifying tower, adopts a plurality of expanders for refrigeration, reduces the energy consumption, and has a large load operating range of the device.
Description
Technical Field
The utility model relates to the technical field of air cryogenic separation, in particular to a liquid oxygen liquefaction air separation device.
Background
Air separation plants provide process gases and liquids to many sectors of the national economy. With the rapid development of various industries, the demand of industrial gas is greatly increased, and especially the demand of liquid products is increased year by year. The liquid product has the advantages of convenience in storage, convenience in supply, quality assurance, high conveying efficiency and the like, is more and more favored by gas manufacturers, the demand of the liquid product rises year by year, and the market potential is very large. The application of full liquid air separation plants has become a trend if the demand of the market cannot be met by only the by-product liquid of the air separation plant.
Firstly, gas-state products are generated, and then a liquefying device is adopted to liquefy the gas-state products according to requirements, so that the energy consumption of the method is relatively high; the other method is to directly adopt a liquid air separation device to produce liquid oxygen and liquid nitrogen products, and compared with the former method, the energy consumption of the method is reduced. Because the liquid air separation plant provides high-grade low-temperature liquid products, the energy consumption of unit products is obviously higher than that of a gas air separation plant, a low-pressure single expansion process is adopted in a conventional small liquefaction device, medium-pressure air is provided with a gas-liquid separator and enters a medium-pressure tower through a throttle valve, the energy consumption is relatively high, so that the key problem in process organization is solved by how to reduce the energy consumption, and the problems of high unit energy consumption, small device load regulation range and the like exist in the conventional all-liquid air separation plant.
SUMMERY OF THE UTILITY MODEL
1. Technical problem to be solved by the utility model
The utility model provides a liquid oxygen liquefaction air separation device, aiming at the technical problems of high unit energy consumption, small device load adjustment range and the like of the existing all-liquid air separation equipment.
2. Technical scheme
In order to solve the problems, the technical scheme provided by the utility model is as follows:
a liquid oxygen liquefaction air separation device comprises an air filter, an air compressor, a precooling module, a purification module, a supercharging end of a supercharging turboexpander, a cooler, a low-temperature air conditioning unit and an expansion end of the supercharging turboexpander which are sequentially connected through pipelines, and further comprises a main heat exchanger, a medium-pressure tower, a condensation evaporator, a low-pressure tower, a subcooler and a fan braking expander, wherein the condensation evaporator is respectively connected with the medium-pressure tower and the low-pressure tower, the cooler and the low-temperature air conditioning unit as well as pipelines between the expansion ends of the low-temperature air conditioning unit and the supercharging turboexpander respectively pass through a refrigeration channel of the main heat exchanger, the expansion end of the supercharging turboexpander is connected with a first pipeline, the first pipeline is connected to the inlet end of the air compressor after passing through a reheating channel of the main heat exchanger, and the outlet end of the purification module is also connected with a second pipeline, the second pipeline is connected with the medium-pressure tower after passing through a refrigeration channel of the main heat exchanger, a liquid-air outlet of the medium-pressure tower is connected with a third pipeline, the third pipeline is connected to the low-pressure tower after passing through the refrigeration channel of the subcooler, a liquid nitrogen outlet of the medium-pressure tower is connected with a fourth pipeline, the fourth pipeline is connected to the low-pressure tower after passing through the refrigeration channel of the subcooler, a liquid oxygen outlet of the condensation evaporator is connected with a fifth pipeline, the fifth pipeline is connected to the storage tank after passing through the refrigeration channel of the subcooler, a waste nitrogen outlet of the medium-pressure tower is connected with a sixth pipeline, and the sixth pipeline is connected to the purification module after sequentially passing through a reheating channel of the subcooler, an expansion end of the fan brake expander and the reheating channel of the main heat exchanger.
Optionally, a first throttle valve is arranged on the third pipeline.
Optionally, a second throttle valve is arranged on the fourth pipeline (.
Optionally, the system further comprises a cold box, and the expansion end of the booster expansion turbine, the expansion end of the fan brake expansion machine (the main heat exchanger, the medium-pressure tower, the condensing evaporator, the low-pressure tower and the subcooler are all arranged in the cold box.
Optionally, the medium pressure column is a sieve plate column or a structured packing column.
Optionally, the lower pressure column is a sieve tray column or a structured packing column.
Optionally, the main heat exchanger, the condensing evaporator and the subcooler are all vacuum brazed plate-fin heat exchangers.
Optionally, the lower pressure column is a pressure column.
3. Advantageous effects
Compared with the prior art, the technical scheme provided by the utility model has the following beneficial effects:
the liquid oxygen liquefaction air separation device directly enters the medium-pressure tower for rectification without arranging a gas-liquid separator and a throttle valve behind the main heat exchanger, the operating pressure of the low-pressure tower is improved as much as possible under the condition of ensuring the heat exchange temperature difference, a gas expander is additionally arranged by utilizing the pressure of the return gas in the low-pressure tower, the refrigeration efficiency of the gas expander is high relative to that of the throttle valve, and the energy consumption of the device is reduced; the novel rectifying tower adopts a newly-added backflow gas expander to replace a medium-pressure air throttle valve, improves the refrigeration efficiency, reduces the energy consumption of the device, fully utilizes the tower-loading pressure by improving the operating pressure of the rectifying tower, adopts a plurality of expanders to refrigerate, reduces the energy consumption, and has a large load operating range of the device.
Drawings
FIG. 1 is a schematic structural diagram of an air separation plant for liquid oxygen liquefaction according to an embodiment of the present invention;
1. an air filter; 2. an air compressor; 3. a pre-cooling module; 4. a purification module; 5. a booster turboexpander; 6. a cooler; 7. a low temperature air conditioning unit; 8. a primary heat exchanger; 9. a medium pressure column; 10. a condensing evaporator; 11. a low pressure column; 12. a subcooler; 13. the fan brakes the expander; 14. a first throttle valve; 15. a second throttle valve; a1, a first pipeline; a2, a second pipeline; a3, a third pipeline; a4, a fourth pipeline; a5, fifth pipeline; a6, sixth pipeline; .
Detailed Description
For a further understanding of the present invention, reference is made to the following detailed description of the utility model taken in conjunction with the accompanying FIG. 1.
With reference to fig. 1, the liquid oxygen liquefaction air separation device of the embodiment includes an air filter 1, an air compressor 2, a pre-cooling module 3, a purification module 4, a pressurization end of a pressurization turbo expander 5, a cooler 6, a low-temperature air conditioning unit 7, an expansion end of the pressurization turbo expander 5, a main heat exchanger 8, a medium-pressure tower 9, a condensation evaporator 10, a low-pressure tower 11, a subcooler 12, and a fan braking expander 12, wherein the condensation evaporator 10 is respectively connected with the medium-pressure tower 9 and the low-pressure tower 11, a refrigeration channel of the condensation evaporator 10 is communicated with a top nitrogen region of the medium-pressure tower 9, an auxiliary heat channel of the condensation evaporator 10 is communicated with a bottom liquid oxygen region of the low-pressure tower 11, pipelines between the cooler 6 and the low-temperature air conditioning unit 7, and pipelines between the expansion ends of the low-temperature air conditioning unit 7 and the pressurization turbo expander 5 respectively pass through a refrigeration channel of the main heat exchanger 8, the expansion end of the booster turboexpander 5 is connected with a first pipeline a1, the first pipeline a1 is connected to the inlet end of the air compressor 2 after passing through the reheating channel of the main heat exchanger 8, the outlet end of the purification module 4 is further connected with a second pipeline a2, the second pipeline a2 is connected with the medium-pressure tower 9 after passing through the refrigerating channel of the main heat exchanger 8, the liquid-air outlet of the medium-pressure tower 9 is connected with a third pipeline a3, the third pipeline a3 is connected to the low-pressure tower 11 after passing through the refrigerating channel of the subcooler 12 (in this embodiment, the third pipeline a3 is provided with a first throttle valve 14), the liquid nitrogen outlet of the medium-pressure tower 9 is connected with a fourth pipeline a4, the fourth pipeline a4 is connected to the low-pressure tower 11 after passing through the refrigerating channel of the subcooler 12 (in this embodiment, the fourth pipeline a4 is provided with a second throttle valve 15), the liquid oxygen outlet of the condensation evaporator 10 is connected with a5, the fifth pipeline a5 is connected to the storage tank after passing through the refrigeration channel of the subcooler 12, the waste nitrogen outlet of the medium-pressure tower 9 is connected with a sixth pipeline a6, and the sixth pipeline a6 is connected to the purification module 4 after sequentially passing through the reheating channel of the subcooler 12, the expansion end of the fan brake expander 12 and the reheating channel of the main heat exchanger 8.
The working principle of the liquid oxygen liquefaction air separation device is as follows: raw material air is filtered by an air filter 1 and then compressed by an air compressor 2, the compressed air with the pressure of 1.0MPa (G) and the temperature of 40 ℃ below zero enters a precooling module to be cooled to 8-17 ℃, the cooled air enters a purification module, water, carbon dioxide and partial hydrocarbon are adsorbed by the purification module, and the gas discharged from the purification module is divided into two parts: one part of the gas enters a supercharging end of a supercharging turbo expander 5, is sent into a cooler 6 after being supercharged, enters a main heat exchanger 8 after being cooled, is subjected to heat exchange with return gas, is extracted from the upper part of the main heat exchanger 8 after being cooled, enters a low-temperature air conditioning unit at the temperature of-10 to-20 ℃ for cooling to-25 to-35 ℃, returns to the main heat exchanger 8 through a pipeline for cooling again to-110 to-120 ℃, then enters an expansion end of the supercharging turbo expander 5 for adiabatic expansion to provide cooling capacity for the whole device, and enters the main heat exchanger for reheating after being expanded, wherein the gas with the pressure of-15 kPa (G) enters an inlet of an air compressor 2 through a first pipeline a 1; the other part of the gas enters a main heat exchanger 8 through a second pipeline a2 to be cooled to be partially liquefied, enters a gas inlet at the lower part of a medium-pressure tower 9 and enters the medium-pressure tower 9 for rectification, and the operating pressure of the medium-pressure tower 9 is 0.95-0.97 MPa (G); oxygen-enriched liquid air is obtained at the bottom of the medium-pressure tower 9, and enters the low-pressure tower 11 to participate in rectification after being subcooled by a subcooler 12 through a third pipeline a 3; obtaining nitrogen at the top of the medium-pressure tower 9, wherein the nitrogen enters a condensation evaporator 10 to be condensed into liquid nitrogen, most of the liquid nitrogen is used as reflux liquid of the medium-pressure tower 9, and the rest of the liquid nitrogen enters a low-pressure tower 11 to participate in rectification after being subcooled by a subcooler through a fourth pipeline a 4; one part of liquid oxygen from the bottom of the low-pressure tower 11 is evaporated in the condensing evaporator 10 to be oxygen which is used as ascending gas of the low-pressure tower 11 to participate in rectification, and the other part of liquid oxygen enters a storage tank after being subcooled by a subcooler through a fifth pipeline a 5; obtaining waste nitrogen with the pressure of 0.13-0.15 MPa (G) at the top of the low-pressure tower 11, reheating the waste nitrogen through a sixth pipeline a6 through a subcooler, and then entering a fan to drive an expansion end of an expansion machine 13 to perform adiabatic expansion so as to provide cold for the whole device; after expansion, the gas with the pressure of 25kPa (G) enters a purification system as regeneration gas after being reheated by a main heat exchanger 8.
The middle pressure tower operating pressure of the conventional liquefaction air separation device is 0.45MPa, the low pressure tower operating pressure is 0.04MPa, the air compressor exhaust pressure is 1.0MPa, (G) partial liquefaction is carried out after the partial liquefaction is carried out of the main heat exchanger, a gas-liquid separator and a throttle valve are required to be arranged for decompressing and entering the middle pressure tower, the liquid oxygen liquefaction air separation device directly enters the middle pressure tower for rectification without arranging the gas-liquid separator and the throttle valve after the main heat exchanger, the low pressure tower operating pressure is improved as much as possible under the condition of ensuring the heat exchange temperature difference, a gas expander is additionally arranged by utilizing the return gas pressure in the low pressure tower, the refrigeration efficiency of the gas expander is high relative to that of the throttle valve, and the energy consumption of the device is reduced; the novel rectifying tower adopts a newly-added backflow gas expander to replace a medium-pressure air throttle valve, improves the refrigeration efficiency, reduces the energy consumption of the device, fully utilizes the tower-loading pressure by improving the operating pressure of the rectifying tower, adopts a plurality of expanders to refrigerate, reduces the energy consumption, and has a large load operating range of the device.
As an alternative of the present invention, the present invention further includes a cold box, wherein the expansion end of the turbo expander 5, the expansion end of the fan brake expander 12, the main heat exchanger 8, the intermediate pressure tower 9, the condensing evaporator 10, the low pressure tower 11 and the subcooler 12 are all installed in the cold box, and the cold box enables the above devices to work in a low temperature environment, so as to ensure the effect of low temperature separation.
As an alternative of the present invention, the medium pressure tower 9 is a sieve plate tower or a structured packing tower, the low pressure tower 11 is a sieve plate tower or a structured packing tower, and the main heat exchanger 8, the condensing evaporator 10 and the subcooler 12 are all vacuum brazed plate-fin heat exchangers, but if the low pressure tower 11 is set as a pressure tower, the liquid oxygen can be discharged from the condensing evaporator 10 and then passes through the cooler 12, and then has sufficient pressure to enter the storage tank.
The present invention and its embodiments have been described above schematically, without limitation, and what is shown in the drawings is only one of the embodiments of the present invention, and the actual structure is not limited thereto. Therefore, if the person skilled in the art receives the teaching, without departing from the spirit of the utility model, the person skilled in the art shall not inventively design the similar structural modes and embodiments to the technical solution, but shall fall within the scope of the utility model.
Claims (8)
1. The utility model provides a liquid oxygen liquefaction air separation plant which characterized in that: the system comprises an air filter, an air compressor, a precooling module, a purification module, a supercharging end of a supercharging turboexpander, a cooler, a low-temperature air conditioning unit and an expansion end of the supercharging turboexpander which are sequentially connected through pipelines, and further comprises a main heat exchanger, a medium-pressure tower, a condensation evaporator, a low-pressure tower, a subcooler and a fan braking expander, wherein the condensation evaporator is respectively connected with the medium-pressure tower and the low-pressure tower, the cooler and the low-temperature air conditioning unit, and pipelines between the low-temperature air conditioning unit and the expansion end of the supercharging turboexpander respectively pass through a refrigeration channel of the main heat exchanger, the expansion end of the supercharging turboexpander is connected with a first pipeline, the first pipeline is connected to the inlet end of the air compressor after passing through a reheating channel of the main heat exchanger, the outlet end of the purification module is also connected with a second pipeline, and the second pipeline is connected with the medium-pressure tower after passing through the refrigeration channel of the main heat exchanger, the liquid-air outlet of the medium-pressure tower is connected with a third pipeline, the third pipeline is connected to the low-pressure tower after passing through a refrigerating channel of a subcooler, a liquid nitrogen outlet of the medium-pressure tower is connected with a fourth pipeline, the fourth pipeline is connected to the low-pressure tower after passing through the refrigerating channel of the subcooler, a liquid oxygen outlet of the condensation evaporator is connected with a fifth pipeline, the fifth pipeline is connected to a storage tank after passing through the refrigerating channel of the subcooler, a waste nitrogen outlet of the medium-pressure tower is connected with a sixth pipeline, and the sixth pipeline is connected to a purification module after sequentially passing through a reheating channel of the subcooler, an expansion end of a fan brake expander and a reheating channel of a main heat exchanger.
2. The liquid oxygen liquefaction air separation plant of claim 1, characterized in that: and a first throttle valve is arranged on the third pipeline.
3. The liquid oxygen liquefaction air separation plant of claim 1, characterized in that: and a second throttle valve is arranged on the fourth pipeline.
4. The liquid oxygen liquefaction air separation plant of any one of claims 1-3, characterized in that: the expansion end of the booster turboexpander, the expansion end of the fan braking expander, the main heat exchanger, the medium-pressure tower, the condensation evaporator, the low-pressure tower and the subcooler are all arranged in the cold box.
5. The liquid oxygen liquefaction air separation plant of claim 4, characterized in that: the medium-pressure tower is a sieve plate tower or a regular packing tower.
6. The liquid oxygen liquefaction air separation plant of claim 4, characterized in that: the low-pressure tower is a sieve plate tower or a regular packing tower.
7. The liquid oxygen liquefaction air separation plant of claim 4, characterized in that: the main heat exchanger, the condensing evaporator and the subcooler are all vacuum brazing plate-fin heat exchangers.
8. The liquid oxygen liquefaction air separation plant of claim 4, characterized in that: the low-pressure tower is a pressure tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123098765.8U CN216522650U (en) | 2021-12-10 | 2021-12-10 | Liquid oxygen liquefaction air separation plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123098765.8U CN216522650U (en) | 2021-12-10 | 2021-12-10 | Liquid oxygen liquefaction air separation plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216522650U true CN216522650U (en) | 2022-05-13 |
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Address after: No. 280 Xingye Road, Leidian Town, Deqing County, Huzhou City, Zhejiang Province, 313200 Patentee after: Yingde Gas Engineering (Zhejiang) Co.,Ltd. Address before: 313200 Jingyi Road, Deqing Linhang Industrial Zone, LEIDIAN Town, Deqing County, Huzhou City, Zhejiang Province Patentee before: ZHEJIANG ZHIHAI CHEMICAL EQUIPMENT ENGINEERING Co.,Ltd. |