CN103062990A - Novel liquid air separation device and process - Google Patents
Novel liquid air separation device and process Download PDFInfo
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- CN103062990A CN103062990A CN2013100267022A CN201310026702A CN103062990A CN 103062990 A CN103062990 A CN 103062990A CN 2013100267022 A CN2013100267022 A CN 2013100267022A CN 201310026702 A CN201310026702 A CN 201310026702A CN 103062990 A CN103062990 A CN 103062990A
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Abstract
The invention discloses a novel 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 the air separation technology field, particularly new liquid air separation unit and technique.
Background technology
At present, many small-sized deep cooling gas space separating devices existed because season and day and night even the difference of day part, the feature that presents fluctuation of user's gas consumption, the per day amount of diffusing of oxygen is larger, thereby causes the operational efficiency of device low, and specific energy consumption is high, cost is high.Be energy efficient, reduce operating cost, increase the enterprise getting profit ability, air separation unit disposes liquefying plant usually, and oxygen, nitrogen with unnecessary emptying are liquefied as liquid oxygen, liquid nitrogen carries out for sale.And institute's dosing gasifying device is outer liquefying plant, exists device varying duty ability bad, and energy consumption is high, and product purity is the difficult problem of nitrogen gas purity control particularly.
Summary of the invention
The object of the invention is to overcome the shortcoming of prior art, a kind of minimizing equipment investment is provided, guarantee simultaneously the output of fluid product and new liquid air separation unit and the technique of purity.
Purpose of the present invention is achieved through the following technical solutions: the new liquid air separation unit, it comprises rectifying column, subcooler, main heat exchanger, decompressor, the circulating nitrogen gas compressor, the liquefaction heat exchanger, the cold gas unit, booster expansion machine, the supercharger aftercooler, rectifying column comprises tower, lower tower and be arranged at Shang Ta and lower tower between the main condenser evaporimeter, the 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, Xia Ta bottom air intlet connects successively, the feeding air runner B of another road of dry air air inlet pipe and main heat exchanger, decompressor, upper tower upper air inlets connects successively, the liquid nitrogen outlet of main condenser evaporimeter is divided into two-way, the liquid nitrogen of main condenser evaporimeter exports one the tunnel and is connected with the liquid nitrogen reflux mouth of lower tower, 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, be connected with the liquid nitrogen product output pipe on the pipeline of the liquid nitrogen runner of connection subcooler and the liquid nitrogen import of upper tower, 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, the outlet of the product nitrogen gas of upper top of tower be divided into two-way after the product nitrogen gas runner of subcooler is connected, the outlet one tunnel of the product nitrogen gas runner of subcooler and the product nitrogen gas runner of main heat exchanger, the product nitrogen gas output pipe connects successively, the product nitrogen gas runner of another road of outlet of the product nitrogen gas runner of subcooler and liquefaction heat exchanger, the circulating nitrogen gas compressor, the pressurized end of booster expansion machine, the supercharger aftercooler, the circulating nitrogen gas air inlet runner of liquefaction heat exchanger, the 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, pipeline connection between the liquid nitrogen runner of the outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger goes out flow channel and the liquid nitrogen outlet that is connected the main condenser evaporimeter and subcooler, the circulating nitrogen gas of the heat exchanger that liquefies goes out another road of outlet of flow channel and the expanding end of booster expansion machine, pipeline between the outlet of the product nitrogen gas runner of connection subcooler and the product nitrogen gas runner of the heat exchanger that is connected connects successively;
The dirty nitrogen outlet that the nearly cat head of upper tower removes is connected successively with the dirty nitrogen runner of subcooler, the dirty nitrogen runner of 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 the pipeline between the oxygen-enriched liquid air runner of described connection subcooler and the oxygen-enriched liquid air import of upper tower, on the pipeline between the liquid nitrogen runner of connection subcooler and the liquid nitrogen import of upper tower, the circulating nitrogen gas that connects the liquefaction heat exchanger goes out on the pipeline between the expanding end of the outlet of flow channel and booster expansion machine, the outlet that the circulating nitrogen gas that connects the liquefaction heat exchanger goes out flow channel export with the liquid nitrogen that is connected the main condenser evaporimeter and the liquid nitrogen runner of subcooler between pipeline on, on the liquid nitrogen product output pipe, on the product nitrogen gas output pipe, on the dirty nitrogen output pipe, be provided with control valve on the product liquid oxygen output pipe He on the oxygen output tube road.
Adopt the space division technique of described new liquid air separation unit, it may further comprise the steps:
S1, raw air are compressed, the cooling purifying is laggard enters main heat exchanger, by product oxygen, product nitrogen gas, the cooling of dirty nitrogen, enter decompressor after the cooling of part raw air, after expander refrigeration, enter tower and participate in rectifying, all the other raw airs are cooled to carry out rectifying near the bottom that enters lower tower behind the dew point;
S2, in rectifying column, air and repeatedly condensation and the evaporation on the multilayer column plate of backflow liquid nitrogen in the lower tower, lower tower bottom gathers oxygen-enriched liquid air, oxygen-enriched liquid air is excessively cold by subcooler, enters Shang Ta through the oxygen-enriched liquid air import of upper tower upper tower cold is provided; The nitrogen of Xia Ta upper end enrichment becomes liquid nitrogen by the main condenser evaporator condensation, and a liquid nitrogen part is further lowered the temperature through condenser, enters top of tower as the withdrawing fluid of upper tower; Another part of liquid nitrogen enters Xia Ta, replenishes cold;
The dirty nitrogen of the portioned product nitrogen of S3, upper top of tower and upper tower middle and upper part enters main heat exchanger through subcooler recovery section cold, obtains product nitrogen gas and dirty nitrogen behind the cooling raw air; The product oxygen of upper tower bottom enters main heat exchanger, and cooling obtains product oxygen behind the raw air, the product liquid oxygen that obtains at the main condenser base of evaporator;
S4, the surplus products nitrogen of upper top of tower is through subcooler recovery section cold, with enter the liquefaction heat exchanger after nitrogen behind the booster expansion machine swell refrigeration mixes, after cooling off by the circulating nitrogen gas compressor compresses, the recovery section cold enters the pressurized end of booster expansion machine, after supercharging, cool off through the supercharger aftercooler again, enter liquefaction heat exchanger heat exchange cooling, enter again the cooling of sub-cooled unit, enter again the liquefaction heat exchanger after the cooling and continue cooling, then part enters the booster expansion machine expanding end, behind the swell refrigeration, and after mixing, product nitrogen gas through subcooler recovery section cold again enters in the liquefaction heat exchanger; Behind all the other liquefaction of nitrogen, the part liquid nitrogen of extracting out with the main condenser evaporimeter be mixed into subcooler cross cold after, part is as nitrogen products output, all the other liquid nitrogen enter top of tower.
The present invention has the following advantages: the present invention is different from existing gas space and divides the varying duty that adds outer liquefying plant flow process, but divide rectifying and heat transmission equipment to organically combine with sky as far as possible, thereby minimizing equipment investment, guarantee simultaneously output and the purity of fluid product, particularly can be in the least possible number of plates situation, improve liquid nitrogen product purity, with suitable market demand.
The present invention can reduce and increase the amount of product liquid oxygen by strengthening or reducing the nitrogen products amount of taking out, and increases simultaneously or reduce oxygen output.Utilize the operating flexibility of air separation unit tower and heat exchanger, reduce oxygen channel setting, liquid nitrogen subcooler and the corresponding instrument setting of liquefying plant part, thus reduce cost.Owing to after the liquefaction of part low-pressure nitrogen is arranged, enter tower and participate in rectifying, thereby can increase the oxygen extraction rate, increase oxygen yield, can improve nitrogen and purity liquid nitrogen, the satisfying the market requirement simultaneously.
The present invention can be in the situation that air demand changes, the consecutive production of implement device and varying duty production, thus reduced energy consumption, the steady quality of while fluid product, guaranteed.
Description of drawings
Fig. 1 is structural representation of the present invention
Among the figure, 1-rectifying column, 2-subcooler, 3-main heat exchanger, 4-decompressor, 5-circulating nitrogen gas compressor, the 6-heat exchanger that liquefies, 7-cold gas unit, 8-booster expansion machine, 9-supercharger aftercooler, the upper tower of 10-, tower under the 11-, 12-main condenser evaporimeter, 13-control valve.
The specific embodiment
The present invention will be further described below in conjunction with accompanying drawing, and protection scope of the present invention is not limited to the following stated:
As shown in Figure 1, the new liquid air separation unit, 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 be arranged at tower 10 and lower tower 11 between main condenser evaporimeter 12, the 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, lower tower 11 bottom air intlets connect 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 connect successively, the liquid nitrogen outlet of main condenser evaporimeter 12 is divided into two-way, the liquid nitrogen of main condenser evaporimeter 12 exports one the tunnel 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, be connected with the liquid nitrogen product output pipe on the pipeline of the liquid nitrogen runner of connection subcooler 2 and the liquid nitrogen import of upper tower 10, the oxygen-enriched liquid air outlet of lower tower 11 bottoms and the oxygen-enriched liquid air runner of subcooler 2, the oxygen-enriched liquid air import of upper tower 10 connects successively, the outlet of the product nitrogen gas at upper tower 10 tops be divided into two-way after the product nitrogen gas runner of subcooler 2 is connected, the outlet one tunnel of the product nitrogen gas runner of subcooler 2 and the product nitrogen gas runner of main heat exchanger 3, the product nitrogen gas output pipe connects successively, the product nitrogen gas runner of another road of outlet of the product nitrogen gas runner of subcooler 2 and 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, pipeline connection between the liquid nitrogen runner of the outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger 6 goes out flow channel and the liquid nitrogen outlet that is connected main condenser evaporimeter 12 and subcooler 2, the circulating nitrogen gas of the heat exchanger 6 that liquefies goes out another road of outlet of flow channel and the expanding end of booster expansion machine 8, pipeline between the outlet of the product nitrogen gas runner of connection subcooler 2 and the product nitrogen gas runner of the heat exchanger 6 that is connected connects successively;
The dirty nitrogen outlet that upper tower 10 nearly cats head remove 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 bottoms connects product liquid oxygen output pipe, and the oxygen outlet of upper tower 10 bottoms is connected successively with main heat exchanger 3 oxygen runners, oxygen output tube road.
On the pipeline between the oxygen-enriched liquid air runner of described connection subcooler 2 and the oxygen-enriched liquid air import of upper tower 10, on the pipeline between the liquid nitrogen runner of connection subcooler 2 and the liquid nitrogen import of upper tower 10, the circulating nitrogen gas that connects liquefaction heat exchanger 6 goes out on the pipeline between the expanding end of the outlet of flow channel and booster expansion machine 8, the outlet that the circulating nitrogen gas that connects liquefaction heat exchanger 6 goes out flow channel export with the liquid nitrogen that is connected main condenser evaporimeter 12 and the liquid nitrogen runner of subcooler 2 between pipeline on, on the liquid nitrogen product output pipe, on the product nitrogen gas output pipe, on the dirty nitrogen output pipe, be provided with control valve 13 on the product liquid oxygen output pipe He on the oxygen output tube road.
Adopt the space division technique of described new liquid air separation unit, it may further comprise the steps:
S1, raw air are compressed, (pressure 5.9bar.A, temperature 287K, flow 8300Nm behind the cooling purifying
3/ h) enter main heat exchanger 3, by product oxygen, product nitrogen gas, the cooling of 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 refrigeration
3/ h), entering tower 10 and participate in rectifying, all the other raw airs are cooled to carry out rectifying near the bottom that enters lower tower 11 behind the dew point;
S2, in rectifying column 1, lower tower 11 interior air and repeatedly condensation and the evaporation on the multilayer column plate of backflow liquid nitrogen, oxygen-enriched liquid air is gathered in lower tower 11 bottoms, and oxygen-enriched liquid air is excessively cold by subcooler 2, enters upper tower 10 through the oxygen-enriched liquid air import of upper tower 10 upper tower 10 colds are provided; The nitrogen of lower tower 11 upper end enrichments is condensed into liquid nitrogen by main condenser evaporimeter 12, and a liquid nitrogen part is further lowered the temperature through condenser, enters tower 10 tops as the withdrawing fluid of upper tower 10; Another part of liquid nitrogen enters lower tower 11, replenishes cold;
The portioned product nitrogen at S3, upper tower 10 tops (pressure 1.35bar.A, temperature 80.2K, flow 3255Nm
3/ h) and the dirty nitrogen of upper tower 10 middle and upper parts through subcooler 2 recovery section colds, enter main heat exchanger 3, obtain product nitrogen gas (pressure 1.1bar.A, temperature 284K, flow 3255Nm behind the cooling raw air
3/ h) and dirty nitrogen; The dirty nitrogen (pressure 1.15bar.A, temperature 284K, the flow 3545Nm that export on the dirty nitrogen output pipe
3/ h) can enter sieve purification system, as regenerating molecular sieve gas; The product oxygen of upper tower 10 bottoms enters main heat exchanger 3, obtains product oxygen (pressure 1.2bar.A, temperature 284K, flow 0Nm behind the cooling raw air
3/ h), the product liquid oxygen (pressure 1.5bar.A, temperature 284K, the flow 1500Nm that obtain in main condenser evaporimeter 12 bottoms
3/ h);
The surplus products nitrogen at S4, upper tower 10 tops (pressure 1.35bar.A, temperature 80.2K, flow 2200 Nm
3/ h) through (pressure 1.3bar.A, temperature 98K, flow 2200Nm behind the subcooler 2 recovery section colds
3/ h), with nitrogen (pressure 1.3bar.A, temperature 80.7K, the flow 10750Nm behind booster expansion machine 8 swell refrigerations
3/ h) mix after (pressure 1.3bar.A, temperature 82.8K, flow 12950Nm
3/ h) enter liquefaction heat exchanger 6, (pressure 1.05bar.A, temperature 310K, flow 12950Nm behind the recovery section cold
3/ h) (pressure 12bar.A, temperature 313K, flow 12950Nm after circulating nitrogen gas compressor 5 compression cooling
3/ h) enter the pressurized end of booster expansion machine 8, after supercharging again through supercharger aftercooler 9 cooling (pressure 16.1bar.A, temperature 313K, flow 12950Nm
3/ h), enter liquefaction heat exchanger 6 heat exchange cooling (pressure 15.9bar.A, temperature 250K, flow 12950Nm
3/ h), enter again the cooling of sub-cooled unit, (pressure 15.8bar.A, temperature 243K, flow 12950Nm after the cooling
3/ h) entering liquefaction heat exchanger 6 continues cooling (pressure 15.7bar.A, temperature 145K, flow 12950Nm again
3/ h), then part enters booster expansion machine 8 expanding ends, (pressure 1.3bar.A, temperature 80.7K, flow 10750Nm behind the swell refrigeration
3/ h), and after mixing, product nitrogen gas through subcooler 2 recovery section colds again enters in the liquefaction heat exchanger 6; (pressure 15.6bar.A, temperature 101.3K, flow 2200Nm behind 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 is as nitrogen products (pressure 1.35bar.A, temperature 77.4K, flow 0Nm
3/ h) output, all the other liquid nitrogen enter tower 10 tops.
Claims (3)
1. new liquid air separation unit, 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 be arranged at tower (10) and lower tower (11) between main condenser evaporimeter (12), the 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), lower tower (11) bottom air intlet 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 one the tunnel 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, be connected with the liquid nitrogen product output pipe on the pipeline of the liquid nitrogen runner of connection subcooler (2) and the liquid nitrogen import of Shang Ta (10), 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 outlet of the product nitrogen gas at upper tower (10) top be divided into two-way after the product nitrogen gas runner of subcooler (2) is connected, the outlet one tunnel of the product nitrogen gas runner of subcooler (2) and the product nitrogen gas runner of main heat exchanger (3), the product nitrogen gas output pipe connects successively, the product nitrogen gas runner of another road of outlet of the product nitrogen gas runner of subcooler (2) and 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, pipeline connection between the liquid nitrogen runner of the outlet one tunnel that the circulating nitrogen gas of liquefaction heat exchanger (6) goes out flow channel and the liquid nitrogen outlet that is connected main condenser evaporimeter (12) and subcooler (2), the circulating nitrogen gas of the heat exchanger (6) that liquefies goes out another road of outlet of flow channel and the expanding end of booster expansion machine (8), pipeline between the outlet of the product nitrogen gas runner of connection subcooler (2) and the product nitrogen gas runner of the heat exchanger that is connected (6) connects successively; The dirty nitrogen outlet that the nearly cat head of upper tower (10) removes 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.
2. new liquid air separation unit according to claim 1 is characterized in that: on the pipeline between the oxygen-enriched liquid air import of the oxygen-enriched liquid air runner of described connection subcooler (2) and Shang Ta (10), on the pipeline between the liquid nitrogen runner of connection subcooler (2) and the liquid nitrogen import of Shang Ta (10), the circulating nitrogen gas that connects liquefaction heat exchanger (6) goes out on the pipeline between the expanding end of the outlet of flow channel and booster expansion machine (8), the outlet that the circulating nitrogen gas that connects liquefaction heat exchanger (6) goes out flow channel export with the liquid nitrogen that is connected main condenser evaporimeter (12) and the liquid nitrogen runner of subcooler (2) between pipeline on, on the liquid nitrogen product output pipe, on the product nitrogen gas output pipe, on the dirty nitrogen output pipe, be provided with control valve (13) on the product liquid oxygen output pipe He on the oxygen output tube road.
3. adopt the space division technique of new liquid air separation unit claimed in claim 1, it is characterized in that: it may further comprise the steps:
S1, raw air are compressed, the cooling purifying is laggard enters main heat exchanger (3), by product oxygen, product nitrogen gas, the cooling of dirty nitrogen, enter decompressor (4) 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 carry out rectifying near the bottom that enters Xia Ta (11) behind the dew point;
S2, in rectifying column (1), the interior air of lower tower (11) and backflow liquid nitrogen be repeatedly condensation and evaporation on the multilayer column plate, oxygen-enriched liquid air is gathered in lower tower (11) bottom, oxygen-enriched liquid air is excessively cold by subcooler (2), enters Shang Ta (10) through the oxygen-enriched liquid air import of upper tower (10) upper tower (10) cold is provided; 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 further lowered the temperature through condenser, enters Shang Ta (10) top as the withdrawing fluid of upper tower (10); Another part of liquid nitrogen enters Xia Ta (11), replenishes cold;
The dirty nitrogen of the portioned product nitrogen at S3, Shang Ta (10) top and upper tower (10) middle and upper part enters main heat exchanger (3) through subcooler (2) recovery section cold, obtains product nitrogen gas and dirty nitrogen behind the cooling raw air; The product oxygen of upper tower (10) bottom enters main heat exchanger (3), obtains product oxygen behind the cooling raw air, the product liquid oxygen that obtains in main condenser evaporimeter (12) bottom;
S4, the surplus products nitrogen at upper tower (10) top is through subcooler (2) recovery section cold, with enter liquefaction heat exchanger (6) after nitrogen behind booster expansion machine (8) swell refrigeration mixes, after cooling off by circulating nitrogen gas compressor (5) compression, the recovery section cold enters the pressurized end of booster expansion machine (8), after supercharging, cool off through supercharger aftercooler (9) again, enter liquefaction heat exchanger (6) heat exchange cooling, enter again the cooling of sub-cooled unit, enter again liquefaction heat exchanger (6) after the cooling and continue cooling, then part enters booster expansion machine (8) expanding end, behind the swell refrigeration, and after mixing, product nitrogen gas through subcooler (2) recovery section cold again enters in the liquefaction heat exchanger (6); Behind 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 is as nitrogen products output, all the other liquid nitrogen enter Shang Ta (10) top.
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| CN104061756A (en) * | 2014-06-09 | 2014-09-24 | 杭州杭氧股份有限公司 | Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting |
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| CN104061756A (en) * | 2014-06-09 | 2014-09-24 | 杭州杭氧股份有限公司 | Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting |
| 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 |
| CN105173016A (en) * | 2015-10-08 | 2015-12-23 | 杜善骥 | Nuclear energy air separation steamship |
| CN106225420A (en) * | 2016-08-19 | 2016-12-14 | 浙江智海化工设备工程有限公司 | A kind of large-scale oxygen/nitrogen liquefaction plant of band deep freeze refrigerator |
| CN107062800A (en) * | 2017-04-21 | 2017-08-18 | 上海启元特种气体发展有限公司 | The method and its device of a kind of superpure nitrogen dehydrogenation |
| CN111542723B (en) * | 2017-12-28 | 2022-04-08 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing air product based on cryogenic rectification process and air separation system |
| CN111542723A (en) * | 2017-12-28 | 2020-08-14 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing air product based on cryogenic rectification process and air separation system |
| CN108413708A (en) * | 2018-06-14 | 2018-08-17 | 上海联风能源科技有限公司 | It is a kind of to improve the method and device for having space division liquid yield |
| CN110160315A (en) * | 2019-06-13 | 2019-08-23 | 兰文旭 | A kind of liquid space division device and production method using night cheap electric power |
| 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 |
| CN115839600A (en) * | 2023-02-22 | 2023-03-24 | 中科富海(杭州)气体工程科技有限公司 | Cryogenic air separation device |
| 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 |
| CN116116034A (en) * | 2023-03-10 | 2023-05-16 | 江南造船(集团)有限责任公司 | Condensation recovery unit |
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