CN103062990B - Liquid air separation device and process - Google Patents
Liquid air separation device and process Download PDFInfo
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- CN103062990B CN103062990B CN201310026702.2A CN201310026702A CN103062990B CN 103062990 B CN103062990 B CN 103062990B CN 201310026702 A CN201310026702 A CN 201310026702A CN 103062990 B CN103062990 B CN 103062990B
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Abstract
The invention discloses a liquid air separation device, which comprises a rectifying tower (1), wherein the rectifying tower (1) comprises an upper tower (10), a lower tower (11) and a main condensation evaporator (12), one path of a product nitrogen outlet of the upper tower (10) is sequentially connected with a main heat exchanger (3) and a product nitrogen output pipeline, and the other path of the product nitrogen outlet is sequentially connected with a liquefaction heat exchanger (6), a circulating nitrogen compressor (5), a pressurization end of a pressurization expander (8), a booster aftercooler (9), the liquefaction heat exchanger (6), a low-temperature air conditioning unit (7) and the liquefaction heat exchanger (6). The invention has the beneficial effects that: the device is organically combined with air separation rectification and heat exchange equipment, so that the equipment investment is reduced, and the yield and the purity of a liquid product are ensured; by increasing or decreasing the liquid nitrogen pumping amount of the product, the amount of liquid oxygen of the product can be reduced and increased, and the oxygen yield is increased or decreased; the continuous production and the variable load production of the device are realized, the energy consumption is reduced, and the product quality is stable and guaranteed.
Description
Technical field
The present invention relates to technical field of air separation, particularly liquid space division device and technique.
Background technology
At present, there is the difference due to season and day and night even day part in many small-sized cryogenic gas air separation units, the feature presenting fluctuation of user's gas consumption, the per day amount of diffusing of oxygen is comparatively large, thus causes the operational efficiency of device low, and specific energy consumption is high, cost is high.For saving energy consumption, reduce operating cost, increase firms profitability, air separation unit configures liquefying plant usually, by the oxygen of unnecessary emptying, nitrogen, is liquefied as liquid oxygen, liquid nitrogen carries out for sale.And institute's dosing gasifying device, be outer liquefying plant, there is device varying duty ability bad, energy consumption is high, and product purity particularly nitrogen gas purity controls difficult problem.
Summary of the invention
The object of the invention is to the shortcoming overcoming prior art, provide a kind of and reduce equipment investment, ensure the output of fluid product and the liquid space division device of purity and technique simultaneously.
Object of the present invention is achieved through the following technical solutions: liquid space division device, and it comprises rectifying column, subcooler, main heat exchanger, decompressor, circulating nitrogen gas compressor, liquefaction heat exchanger, cold gas unit, booster expansion machine, supercharger aftercooler, rectifying column comprises tower, lower tower and the main condenser evaporimeter be arranged between Shang Ta and lower tower, dry air air inlet pipe is divided into two-way, the feeding air runner A of dry air air inlet pipe one tunnel and main heat exchanger, the import of lower tower lower air connects successively, another road of dry air air inlet pipe and the feeding air runner B of main heat exchanger, decompressor, upper tower upper air inlets connects successively, and the liquid nitrogen outlet of main condenser evaporimeter is divided into two-way, and the liquid nitrogen of main condenser evaporimeter exports a road and is connected with the liquid nitrogen reflux mouth of lower tower, and the liquid nitrogen of main condenser evaporimeter exports the liquid nitrogen runner of another road and subcooler, the liquid nitrogen import of upper tower connects successively, and the pipeline of the connection liquid nitrogen runner of subcooler and the liquid nitrogen import of upper tower is connected with liquid nitrogen product output pipe, the oxygen-enriched liquid air outlet of lower tower bottom and the oxygen-enriched liquid air runner of subcooler, the oxygen-enriched liquid air import of upper tower connects successively, and the product nitrogen gas of upper top of tower is divided into two-way, outlet one tunnel of the product nitrogen gas runner of subcooler and the product nitrogen gas runner of main heat exchanger after exporting and being connected with the product nitrogen gas runner of subcooler, product nitrogen gas output pipe connects successively, another road of outlet of the product nitrogen gas runner of subcooler and the product nitrogen gas runner of liquefaction heat exchanger, circulating nitrogen gas compressor, the pressurized end of booster expansion machine, supercharger aftercooler, the circulating nitrogen gas air inlet runner of liquefaction heat exchanger, cold gas unit, the circulating nitrogen gas of liquefaction heat exchanger goes out flow channel and connects successively, the outlet that the circulating nitrogen gas of liquefaction heat exchanger goes out flow channel is divided into two-way, outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger goes out flow channel connects with the pipeline that the liquid nitrogen being connected main condenser evaporimeter exports between the liquid nitrogen runner of subcooler, and the circulating nitrogen gas of liquefaction heat exchanger goes out another road of outlet of flow channel and the expanding end of booster expansion machine, the pipeline connected between the outlet of product nitrogen gas runner of subcooler and the product nitrogen gas runner of liquefaction heat exchanger is connected successively,
The dirty nitrogen outlet at upper tower nearly tower top place is connected successively with the dirty nitrogen runner of the dirty nitrogen runner of subcooler, main heat exchanger, dirty nitrogen output pipe; The product liquid oxygen outlet of main condenser base of evaporator connects product liquid oxygen output pipe, and the oxygen outlet of upper tower bottom is connected successively with main heat exchanger oxygen runner, oxygen output tube road.
On pipeline between the oxygen-enriched liquid air runner of described connection subcooler and the oxygen-enriched liquid air import of upper tower, connect on the pipeline between the liquid nitrogen runner of subcooler and the liquid nitrogen import of upper tower, the circulating nitrogen gas connecting liquefaction heat exchanger goes out on the pipeline between the outlet of flow channel and the expanding end of booster expansion machine, connecting the outlet that the circulating nitrogen gas of liquefaction heat exchanger goes out flow channel exports on the pipeline between the liquid nitrogen runner of subcooler with the liquid nitrogen being connected main condenser evaporimeter, on liquid nitrogen product output pipe, on product nitrogen gas output pipe, on dirty nitrogen output pipe, control valve is provided with on product liquid oxygen output pipe He on oxygen output tube road.
The space division technique of the liquid space division device described in employing, it comprises the following steps:
S1, raw air be compressed, cooling purifying laggard enter main heat exchanger, cooled by product oxygen, product nitrogen gas, dirty nitrogen, decompressor is entered after the cooling of part raw air, after expander refrigeration, enter tower and participate in rectifying, all the other raw airs are cooled to the bottom close to entering lower tower after dew point, carry out rectifying;
S2, in rectifying column, air and backflow liquid nitrogen condensation and evaporation repeatedly on multilayer column plate in lower tower, lower tower bottom gathers oxygen-enriched liquid air, and oxygen-enriched liquid air is excessively cold by subcooler, and the oxygen-enriched liquid air import through upper tower enters Shang Ta and provides upper tower cold; The nitrogen of Xia Ta upper end enrichment becomes liquid nitrogen by main condenser evaporator condensation, and a liquid nitrogen part is lowered the temperature further through subcooler, enters the withdrawing fluid of top of tower as upper tower; Another part of liquid nitrogen enters Xia Ta, supplements cold;
The portioned product nitrogen of S3, upper top of tower and the dirty nitrogen of upper tower middle and upper part, through subcooler recovery section cold, enter main heat exchanger, obtain product nitrogen gas and dirty nitrogen after cooling raw air; The product oxygen of upper tower bottom enters main heat exchanger, obtains product oxygen, at the product liquid oxygen that main condenser base of evaporator obtains after cooling raw air;
S4, the surplus products nitrogen of upper top of tower is through subcooler recovery section cold, liquefaction heat exchanger is entered after mixing with the nitrogen after booster expansion machine swell refrigeration, after the cooling of circulating nitrogen gas compressor compresses, the pressurized end of booster expansion machine is entered after recovery section cold, cool through supercharger aftercooler again after supercharging, enter liquefaction heat exchanger heat exchange cooling, enter the cooling of sub-cooled unit again, enter liquefaction heat exchanger after cooling again and continue cooling, then part enters booster expansion machine expanding end, after swell refrigeration, again enter in liquefaction heat exchanger after mixing through the product nitrogen gas of subcooler recovery section cold, after all the other liquefaction of nitrogen, the part liquid nitrogen of extracting out with main condenser evaporimeter be mixed into subcooler cross cold after, part as nitrogen products export, all the other liquid nitrogen enter top of tower.
The present invention has the following advantages: the present invention is different from the varying duty flow process that existing gas space divides additional outer liquefying plant, but divide rectifying and heat transmission equipment to organically combine as far as possible with sky, thus minimizing equipment investment, ensure output and the purity of fluid product simultaneously, particularly can in the least possible number of plates situation, improve liquid nitrogen product purity, with suitable market demand.
The present invention, by strengthening or reducing the nitrogen products amount of taking out, can reduce and increase the amount of product liquid oxygen, increases simultaneously or reduces oxygen output.Utilize the operating flexibility of air separation unit tower and heat exchanger, reduce the oxygen channel setting of liquefying plant part, liquid nitrogen subcooler and corresponding instrument and arrange, thus reduce investment.Owing to there being part low-pressure nitrogen post liquefaction, entering tower and participate in rectifying, thus oxygen extraction rate can be increased, increase oxygen yield, nitrogen and purity liquid nitrogen can be improved simultaneously, meet market demands.
The present invention can when air demand changes, and the consecutive production of implement device and varying duty are produced, thus reduce energy consumption, simultaneously the steady quality, guaranteed of fluid product.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention
In figure, 1-rectifying column, 2-subcooler, 3-main heat exchanger, 4-decompressor, 5-circulating nitrogen gas compressor, 6-liquefaction heat exchanger, 7-cold gas unit, 8-booster expansion machine, 9-supercharger aftercooler, the upper tower of 10-, tower under 11-, 12-main condenser evaporimeter, 13-control valve.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention will be further described, and protection scope of the present invention is not limited to the following stated:
As shown in Figure 1, liquid space division device, it comprises rectifying column 1, subcooler 2, main heat exchanger 3, decompressor 4, circulating nitrogen gas compressor 5, liquefaction heat exchanger 6, cold gas unit 7, booster expansion machine 8, supercharger aftercooler 9, rectifying column 1 comprises tower 10, lower tower 11 and the main condenser evaporimeter 12 be arranged between tower 10 and lower tower 11, dry air air inlet pipe is divided into two-way, the feeding air runner A of dry air air inlet pipe one tunnel and main heat exchanger 3, the import of lower tower 11 lower air connects successively, another road of dry air air inlet pipe and the feeding air runner B of main heat exchanger 3, decompressor 4, upper tower 10 upper air inlets connects successively, the liquid nitrogen outlet of main condenser evaporimeter 12 is divided into two-way, the liquid nitrogen of main condenser evaporimeter 12 exports a road and is connected with the liquid nitrogen reflux mouth of lower tower 11, the liquid nitrogen of main condenser evaporimeter 12 exports the liquid nitrogen runner of another road and subcooler 2, the liquid nitrogen import of upper tower 10 connects successively, the pipeline of the connection liquid nitrogen runner of subcooler 2 and the liquid nitrogen import of upper tower 10 is connected with liquid nitrogen product output pipe, oxygen-enriched liquid air outlet bottom lower tower 11 and the oxygen-enriched liquid air runner of subcooler 2, the oxygen-enriched liquid air import of upper tower 10 connects successively, the product nitrogen gas at upper tower 10 top is divided into two-way after exporting and being connected with the product nitrogen gas runner of subcooler 2, outlet one tunnel of the product nitrogen gas runner of subcooler 2 and the product nitrogen gas runner of main heat exchanger 3, product nitrogen gas output pipe connects successively, another road of outlet of the product nitrogen gas runner of subcooler 2 and the product nitrogen gas runner of liquefaction heat exchanger 6, circulating nitrogen gas compressor 5, the pressurized end of booster expansion machine 8, supercharger aftercooler 9, the circulating nitrogen gas air inlet runner of liquefaction heat exchanger 6, cold gas unit 7, the circulating nitrogen gas of liquefaction heat exchanger 6 goes out flow channel and connects successively, the outlet that the circulating nitrogen gas of liquefaction heat exchanger 6 goes out flow channel is divided into two-way, outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger 6 goes out flow channel connects with the pipeline that the liquid nitrogen being connected main condenser evaporimeter 12 exports between the liquid nitrogen runner of subcooler 2, the circulating nitrogen gas of liquefaction heat exchanger 6 goes out another road of outlet of flow channel and the expanding end of booster expansion machine 8, the pipeline connected between the outlet of product nitrogen gas runner of subcooler 2 and the product nitrogen gas runner of liquefaction heat exchanger 6 is connected successively,
The dirty nitrogen outlet at the nearly tower top place of upper tower 10 is connected successively with the dirty nitrogen runner of subcooler 2, the dirty nitrogen runner of main heat exchanger 3, dirty nitrogen output pipe; Product liquid oxygen outlet bottom main condenser evaporimeter 12 connects product liquid oxygen output pipe, and the oxygen outlet bottom upper tower 10 is connected successively with main heat exchanger 3 oxygen runner, oxygen output tube road.
On pipeline between the oxygen-enriched liquid air runner of described connection subcooler 2 and the oxygen-enriched liquid air import of upper tower 10, connect on the pipeline between the liquid nitrogen runner of subcooler 2 and the liquid nitrogen import of upper tower 10, the circulating nitrogen gas connecting liquefaction heat exchanger 6 goes out on the pipeline between the outlet of flow channel and the expanding end of booster expansion machine 8, connecting the outlet that the circulating nitrogen gas of liquefaction heat exchanger 6 goes out flow channel exports on the pipeline between the liquid nitrogen runner of subcooler 2 with the liquid nitrogen being connected main condenser evaporimeter 12, on liquid nitrogen product output pipe, on product nitrogen gas output pipe, on dirty nitrogen output pipe, control valve 13 is provided with on product liquid oxygen output pipe He on oxygen output tube road.
The space division technique of the liquid space division device described in employing, it comprises the following steps:
S1, raw air be compressed, (pressure 5.9bar.A, temperature 287K, flow 8300Nm after cooling purifying
3/ h) enter main heat exchanger 3, cooled by product oxygen, product nitrogen gas, dirty nitrogen, (pressure 5.8bar.A, temperature 148K, flow 1500Nm after a part of raw air cooling
3/ h) enter decompressor 4, (pressure 1.5bar.A, temperature 107K, flow 1500Nm after decompressor 4 freezes
3/ h), enter tower 10 and participate in rectifying, all the other raw airs are cooled to, close to the bottom entering lower tower 11 after dew point, carry out rectifying;
S2, in rectifying column 1, air and condensation and the evaporation repeatedly on multilayer column plate of backflow liquid nitrogen in lower tower 11, gather oxygen-enriched liquid air bottom lower tower 11, oxygen-enriched liquid air is excessively cold by subcooler 2, and the oxygen-enriched liquid air import through upper tower 10 enters upper tower 10 and provides upper tower 10 cold; The nitrogen of lower tower 11 upper end enrichment is condensed into liquid nitrogen by main condenser evaporimeter 12, and a liquid nitrogen part is lowered the temperature further through subcooler 2, enters the withdrawing fluid of tower 10 top as upper tower 10; Another part of liquid nitrogen enters lower tower 11, supplements cold;
Portioned product nitrogen (pressure 1.35bar.A, temperature 80.2K, the flow 3255Nm at S3, upper tower 10 top
3/ h) and the dirty nitrogen of upper tower 10 middle and upper part through subcooler 2 recovery section cold, enter main heat exchanger 3, after cooling raw air, obtain product nitrogen gas (pressure 1.1bar.A, temperature 284K, flow 3255Nm
3/ h) and dirty nitrogen; Dirty nitrogen (pressure 1.15bar.A, temperature 284K, flow 3545Nm that dirty nitrogen output pipe exports
3/ h) can sieve purification system be entered, as regenerating molecular sieve gas; Product oxygen bottom upper tower 10 enters main heat exchanger 3, obtains product oxygen (pressure 1.2bar.A, temperature 284K, flow 0Nm after cooling raw air
3/ h), the product liquid oxygen (pressure 1.5bar.A, temperature 284K, the flow 1500Nm that obtain bottom main condenser evaporimeter 12
3/ h);
Surplus products nitrogen (pressure 1.35bar.A, temperature 80.2K, flow 2200 Nm at S4, upper tower 10 top
3/ h) (pressure 1.3bar.A, temperature 98K, flow 2200Nm after subcooler 2 recovery section cold
3/ h), with nitrogen (pressure 1.3bar.A, temperature 80.7K, the flow 10750Nm after booster expansion machine 8 swell refrigeration
3/ h) mixing rear (pressure 1.3bar.A, temperature 82.8K, flow 12950Nm
3/ h) enter liquefaction heat exchanger 6, (pressure 1.05bar.A, temperature 310K, flow 12950Nm after recovery section cold
3/ h) compress (pressure 12bar.A, temperature 313K, flow 12950Nm after cooling through circulating nitrogen gas compressor 5
3/ h) enter the pressurized end of booster expansion machine 8, after supercharging, cool (pressure 16.1bar.A, temperature 313K, flow 12950Nm through supercharger aftercooler 9 again
3/ h), enter liquefaction heat exchanger 6 heat exchange cooling (pressure 15.9bar.A, temperature 250K, flow 12950Nm
3/ h), then enter the cooling of sub-cooled unit, (pressure 15.8bar.A, temperature 243K, flow 12950Nm after cooling
3/ h) enter liquefaction heat exchanger 6 continuation cooling (pressure 15.7bar.A, temperature 145K, flow 12950Nm again
3/ h), then part enters booster expansion machine 8 expanding end, (pressure 1.3bar.A, temperature 80.7K, flow 10750Nm after swell refrigeration
3/ h), again enter in liquefaction heat exchanger 6 after mixing through the product nitrogen gas of subcooler 2 recovery section cold; (pressure 15.6bar.A, temperature 101.3K, flow 2200Nm after all the other liquefaction of nitrogen
3/ h), the part liquid nitrogen of extracting out with main condenser evaporimeter 12 be mixed into subcooler 2 cross cold after, part as nitrogen products (pressure 1.35bar.A, temperature 77.4K, flow 0Nm
3/ h) export, all the other liquid nitrogen enter tower 10 top.
Claims (2)
1. liquid space division device, it is characterized in that: it comprises rectifying column (1), subcooler (2), main heat exchanger (3), decompressor (4), circulating nitrogen gas compressor (5), liquefaction heat exchanger (6), cold gas unit (7), booster expansion machine (8), supercharger aftercooler (9), rectifying column (1) comprises tower (10), lower tower (11) and the main condenser evaporimeter (12) be arranged between tower (10) and lower tower (11), dry air air inlet pipe is divided into two-way, the feeding air runner A of dry air air inlet pipe one tunnel and main heat exchanger (3), the lower air import of lower tower (11) connects successively, the feeding air runner B of another road of dry air air inlet pipe and main heat exchanger (3), decompressor (4), upper tower (10) upper air inlets connects successively, the liquid nitrogen outlet of main condenser evaporimeter (12) is divided into two-way, the liquid nitrogen of main condenser evaporimeter (12) exports a road and is connected with the liquid nitrogen reflux mouth of Xia Ta (11), the liquid nitrogen of main condenser evaporimeter (12) exports the liquid nitrogen runner of another road and subcooler (2), the liquid nitrogen import of upper tower (10) connects successively, the pipeline of the liquid nitrogen runner of connection subcooler (2) and the liquid nitrogen import of Shang Ta (10) is connected with liquid nitrogen product output pipe, the oxygen-enriched liquid air outlet of lower tower (11) bottom and the oxygen-enriched liquid air runner of subcooler (2), the oxygen-enriched liquid air import of upper tower (10) connects successively, the product nitrogen gas at upper tower (10) top is divided into two-way after exporting and being connected with the product nitrogen gas runner of subcooler (2), outlet one tunnel of the product nitrogen gas runner of subcooler (2) and the product nitrogen gas runner of main heat exchanger (3), product nitrogen gas output pipe connects successively, another road of outlet of the product nitrogen gas runner of subcooler (2) and the product nitrogen gas runner of liquefaction heat exchanger (6), circulating nitrogen gas compressor (5), the pressurized end of booster expansion machine (8), supercharger aftercooler (9), the circulating nitrogen gas air inlet runner of liquefaction heat exchanger (6), cold gas unit (7), the circulating nitrogen gas of liquefaction heat exchanger (6) goes out flow channel and connects successively, the outlet that the circulating nitrogen gas of liquefaction heat exchanger (6) goes out flow channel is divided into two-way, outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger (6) goes out flow channel connects with the pipeline that the liquid nitrogen being connected main condenser evaporimeter (12) exports between the liquid nitrogen runner of subcooler (2), the circulating nitrogen gas of liquefaction heat exchanger (6) goes out another road of outlet of flow channel and the expanding end of booster expansion machine (8), the pipeline connected between the outlet of product nitrogen gas runner of subcooler (2) and the product nitrogen gas runner of liquefaction heat exchanger (6) is connected successively, the dirty nitrogen outlet at the nearly tower top place of upper tower (10) is connected successively with the dirty nitrogen runner of subcooler (2), the dirty nitrogen runner of main heat exchanger (3), dirty nitrogen output pipe, the product liquid oxygen outlet of main condenser evaporimeter (12) bottom connects product liquid oxygen output pipe, and the oxygen outlet of upper tower (10) bottom is connected successively with main heat exchanger (3) oxygen runner, oxygen output tube road,
The space division technique of the liquid space division device described in employing, it comprises the following steps:
S1, raw air be compressed, cooling purifying laggard enter main heat exchanger (3), cooled by product oxygen, product nitrogen gas, dirty nitrogen, decompressor (4) is entered after the cooling of part raw air, after decompressor (4) refrigeration, enter Shang Ta (10) and participate in rectifying, all the other raw airs are cooled to the bottom close to entering Xia Ta (11) after dew point, carry out rectifying;
S2, in rectifying column (1), the interior air of lower tower (11) and condensation and the evaporation repeatedly on multilayer column plate of backflow liquid nitrogen, oxygen-enriched liquid air is gathered in lower tower (11) bottom, oxygen-enriched liquid air is excessively cold by subcooler (2), and the oxygen-enriched liquid air import through upper tower (10) enters Shang Ta (10) and provides upper tower (10) cold; The nitrogen of lower tower (11) upper end enrichment is condensed into liquid nitrogen by main condenser evaporimeter (12), and a liquid nitrogen part is lowered the temperature further through subcooler (2), enters the withdrawing fluid of Shang Ta (10) top as upper tower (10); Another part of liquid nitrogen enters Xia Ta (11), supplements cold;
The portioned product nitrogen at S3, Shang Ta (10) top and the dirty nitrogen of upper tower (10) middle and upper part, through subcooler (2) recovery section cold, enter main heat exchanger (3), obtain product nitrogen gas and dirty nitrogen after cooling raw air; The dirty nitrogen that dirty nitrogen output pipe exports enters sieve purification system, as regenerating molecular sieve gas; The product oxygen of upper tower (10) bottom enters main heat exchanger (3), obtains product oxygen after cooling raw air, at the product liquid oxygen that main condenser evaporimeter (12) bottom obtains;
S4, the surplus products nitrogen at upper tower (10) top is through subcooler (2) recovery section cold, liquefaction heat exchanger (6) is entered after mixing with the nitrogen after booster expansion machine (8) swell refrigeration, after circulating nitrogen gas compressor (5) compression cooling, the pressurized end of booster expansion machine (8) is entered after recovery section cold, cool through supercharger aftercooler (9) again after supercharging, enter liquefaction heat exchanger (6) heat exchange cooling, enter the cooling of sub-cooled unit again, enter liquefaction heat exchanger (6) after cooling again and continue cooling, then part enters booster expansion machine (8) expanding end, after swell refrigeration, again enter in liquefaction heat exchanger (6) after mixing through the product nitrogen gas of subcooler (2) recovery section cold, after all the other liquefaction of nitrogen, the part liquid nitrogen of extracting out with main condenser evaporimeter (12) be mixed into subcooler (2) cross cold after, part as nitrogen products export, all the other liquid nitrogen enter Shang Ta (10) top.
2. liquid space division device according to claim 1, it is characterized in that: on the pipeline between the oxygen-enriched liquid air runner of described connection subcooler (2) and the oxygen-enriched liquid air import of Shang Ta (10), connect on the pipeline between the liquid nitrogen runner of subcooler (2) and the liquid nitrogen import of Shang Ta (10), the circulating nitrogen gas connecting liquefaction heat exchanger (6) goes out on the pipeline between the outlet of flow channel and the expanding end of booster expansion machine (8), the outlet that the circulating nitrogen gas connecting liquefaction heat exchanger (6) goes out flow channel exports on the pipeline between the liquid nitrogen runner of subcooler (2) with the liquid nitrogen being connected main condenser evaporimeter (12), on liquid nitrogen product output pipe, on product nitrogen gas output pipe, on dirty nitrogen output pipe, control valve (13) is provided with on product liquid oxygen output pipe He on oxygen output tube road.
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| CN105758119A (en) * | 2014-12-19 | 2016-07-13 | 常熟市永安工业气体制造有限公司 | Liquid oxygen preparation device |
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| CN110160315B (en) * | 2019-06-13 | 2024-04-12 | 兰文旭 | Liquid air separation device utilizing low-cost night electric power and production method |
| CN112325567A (en) * | 2020-11-05 | 2021-02-05 | 常德天盛电化有限公司 | Liquid nitrogen preparation system |
| CN113606866A (en) * | 2021-08-06 | 2021-11-05 | 苏州市兴鲁空分设备科技发展有限公司 | Device and method for preparing nitrogen by air separation |
| CN115839600B (en) * | 2023-02-22 | 2023-05-05 | 中科富海(杭州)气体工程科技有限公司 | Cryogenic air separation plant |
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