CN102320581A - A kind of nitrogen reparation technology - Google Patents
A kind of nitrogen reparation technology Download PDFInfo
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- CN102320581A CN102320581A CN201110252527A CN201110252527A CN102320581A CN 102320581 A CN102320581 A CN 102320581A CN 201110252527 A CN201110252527 A CN 201110252527A CN 201110252527 A CN201110252527 A CN 201110252527A CN 102320581 A CN102320581 A CN 102320581A
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/0423—Subcooling of liquid process streams
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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.
- F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
- F25J3/044—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 single pressure main column system only
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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
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
Abstract
The invention belongs to the air separation technology field, particularly a kind of nitrogen reparation technology.Said nitrogen reparation technology comprises removal of impurities, compression, precooling, the purification of air successively, and rectifying was carried out in entering rectifying tower bottom after cleaned air passes was cooled to temperature of saturation, obtained nitrogen at the rectifying tower top.The row pressure of this process air compressor is low, energy consumption is low, greatly reduces the energy consumption requirement of nitrogen production by air separation device, meets the requirement of the present energy-saving and emission-reduction to high energy-consuming industry of country, and the nitrogen extraction yield can reach 45-65% simultaneously.
Description
Technical field
The invention belongs to the air separation technology field, particularly a kind of nitrogen reparation technology.
Background technology
Along with The development in society and economy, in recent years, the Application Areas of high-purity nitrogen plant is constantly expanded, and all has like industries such as petrochemical industry, glass, rubber, building board, polysilicon, thomels to set foot in.Industry is ever-increasing to the demand of nitrogen, simultaneously to the energy-saving and cost-reducing also constantly higher requirement of proposition.Therefore, want on market, to occupy whip hand, just must improve product extraction rate, reduce the operation energy consumption of device, the energy-saving potential of excavating equipment operation is researched and developed new nitrogen producing craft simultaneously.
Summary of the invention
The object of the present invention is to provide a kind of nitrogen reparation technology, overcome that present handicraft product extraction yield is low, device operation energy consumption bigger defective.
The technical scheme that the present invention adopts is following:
A kind of nitrogen reparation technology comprises removal of impurities, compression, precooling, the purification of air successively, and rectifying was carried out in entering rectifying tower bottom after cleaned air passes was cooled to temperature of saturation, obtained nitrogen at the rectifying tower top.
After the oxygen-enriched liquid air that rectifier bottoms obtains passed through cold throttling, get into the condenser/evaporator and the nitrogen phase-change heat-exchange of rectifying tower top portion after the rectifying, the liquid nitrogen that condensation obtains partly returns rectifying tower as phegma, and part is seen off as liquid nitrogen product.
Through supercooler, main heat exchanger re-heat, go turbo-expander to expand afterwards after drawing from condenser/evaporator as waste gas with the air behind the nitrogen phase-change heat-exchange.
The back waste gas that expands gets into main heat exchanger and cleaned air passes heat exchange, and the heat exchange rear section is as the purification system resurgent gases.
The nitrogen that the rectifying tower top obtains goes out that rectifying tower is laggard delivers to the user after going into main heat exchanger re-heat to normal temperature.
Those skilled in the art are according to arts demand, also can adjust the back waste gas that expands and get into and get into main heat exchanger again behind the supercooler and carry out heat exchange.
The air compression of wherein mentioning generally is compressed to than product nitrogen gas and requires the high 70-95Kpa of pressure.
The extraction yield of above technology nitrogen is 45-58%, and the nitrogen pressure of acquisition (being nitrogen product requirement pressure) is 450-1100Kpa, in the nitrogen 0
2Be 1-100ppm.
The present invention also further provides two kinds of more energy-saving and cost-reducing preferred versions:
1) is compressed to after the air removal of impurities than the low 40-100Kpa of product nitrogen gas requirement pressure; Before cleaned air passes entering main heat exchanger was cooled, supercharging once more was to requiring the high 30-40Kpa of pressure than product nitrogen gas.
Concrete, the pressurized end that cleaned air passes can get into the booster expansion turbine group carries out supercharging.
The preferred theoretical plate number that adopts is that the structured packing rectifying tower that 60-90 or corresponding filler 60-120 coil carries out rectifying.
This programme is the 10-12% of basic technology with respect to the inlet amount that aforesaid basic technology can reduce raw air, with further raising extraction yield.
2) be compressed to after the air removal of impurities than the low 100-180Kpa of product nitrogen gas requirement pressure; The nitrogen that the rectifying tower top obtains goes out that rectifying tower is laggard to be gone into to be pressurized to product nitrogen gas behind main heat exchanger re-heat to the normal temperature and to require pressure to deliver to the user.
Concrete, can carry out supercharging through the pressurized end that gets into the booster expansion turbine group behind re-heat to the normal temperature.
The preferred theoretical plate number that adopts is that the structured packing rectifying tower that 60-90 or corresponding filler 60-120 coil carries out rectifying.
This programme is 15% of a basic technology with respect to the inlet amount that aforesaid basic technology can reduce raw air, with further raising extraction yield.
Specifically set forth in the face of technology of the present invention down:
1. basic technology: raw air is removed koniology and impurity through air filter; Be compressed to than the high 70-95Kpa of nitrogen product requirement pressure by air then; Reducing AT through chilldown system again is 5-8 ℃, gets into purification system after separating free-water, removes H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes is carried out heat exchange and is cooled to temperature of saturation through main heat exchanger and expansion waste gas and nitrogen, gets into the rectifying tower bottom and participates in rectifying.Obtain high pure nitrogen at the rectifying tower top, the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower gets into condenser/evaporator and nitrogen phase-change heat-exchange through the supercooler throttling, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler, main heat exchanger re-heat, is gone turbo-expander to expand; Increase cold to the device benefit, expansion waste gas optionally passes through supercooler according to arts demand, passes through the main heat exchanger re-heat afterwards to normal temperature; Part is as the purification system resurgent gases, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower top, sees off to the user through main heat exchange re-heat to normal temperature and uses, and the nitrogen product pressure of acquisition just meets the requirements.Adopt this technology, the nitrogen pressure that is delivered to user side is generally at 450-1100KPa (G), and nitrogen gas purity is O
2Be 1-100ppm.
Below two schemes can further cut down the consumption of energy, increase the nitrogen pressure can be delivered to user side simultaneously or obtain liquid nitrogen product at user side:
Concrete, scheme one is following:
Raw air (inlet amount can reduce 10-12% than basic technology) is removed koniology and impurity through air filter; Be compressed to than behind the low 40-100Kpa of nitrogen product requirement pressure (can save energy consumption 15% here) by air then; Reduce AT through chilldown system again; Get into purification system after separating free-water, remove H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes gets into the pressurized end of booster expansion turbine group, behind the pressurize (requiring the high 30-40Kpa of pressure than nitrogen product), carries out heat exchange and is cooled to temperature of saturation through main heat exchanger and expansion waste gas and nitrogen, gets into the participation rectifying of rectifying tower bottom.Rectifying tower adopts regular packed tower (number of theoretical plate 60-90 piece), obtains high pure nitrogen (pressure satisfies nitrogen product requirement pressure) at the rectifying tower top, and the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower flows into condenser/evaporator and nitrogen phase-change heat-exchange through cold deutomerite, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler, main heat exchanger re-heat, is gone turbo-expander to expand; Increase cold to the device benefit; To normal temperature, part is as the purification system resurgent gases through supercooler (optionally passing through according to arts demand), main heat exchanger re-heat for expansion waste gas, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower top, sees off through main heat exchange re-heat to normal temperature.
This technology nitrogen output>=5000Nm
3/ h, nitrogen gas purity can reach O
2≤3ppm, this technology can make the row pressure of pneumatics unit reduce 100-150Kpa; Nitrogen extraction rate reached 55-70%, system nitrogen power consumption is 0.22kwh/Nm
3N
2
Concrete, the flow process of technical scheme two is following:
Raw air (inlet amount can reduce by 15% than basic technology) is removed koniology and impurity through air filter; Be compressed to than behind the low 100-180Kpa of nitrogen product requirement pressure (energy consumption reduces 18-20%) here by air then; Again after chilldown system reduces AT; Get into purification system after separating free-water, remove H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes is carried out heat exchange and is cooled to temperature of saturation through main heat exchanger and expansion waste gas and nitrogen, gets into the rectifying tower bottom and participates in rectifying.Rectifying tower adopts regular packed tower, number of theoretical plate 60-90 piece (filler 60-120 dish); Obtain high pure nitrogen (pressure requires the low about 100-180Kpa of pressure than nitrogen product) at the rectifying tower top, the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower flows into condenser/evaporator and nitrogen phase-change heat-exchange through cold deutomerite, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler, main heat exchanger re-heat, is gone turbo-expander to expand; Increase cold to the device benefit; To normal temperature, part is as the purification system resurgent gases through supercooler (optionally passing through according to arts demand), main heat exchanger re-heat for expansion waste gas, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower top; Get into the pressurized end of booster expansion turbine group through main heat exchange re-heat to normal temperature; Pressurize to nitrogen product requires to send the user behind the pressure; This technology can make the relative basic technology row pressure of pneumatics unit reduce about 200Kpa, and the related rectifying tower pressure that reduced improves separation efficiency.
This technology nitrogen output>=5000Nm
3/ h, nitrogen gas purity 10ppm>=O
2>=3ppm.Nitrogen extraction rate reached 55-65%, energy consumption is 0.21kwh/Nm
3N
2
The present invention has following advantage with respect to prior art:
Nitrogen reparation technology air of the present invention row pressure is low, and energy consumption is low, greatly reduces the energy consumption requirement of nitrogen production by air separation device, meets the requirement of the present energy-saving and emission-reduction to high energy-consuming industry of country, and the nitrogen extraction yield can reach 55-70% simultaneously.
Description of drawings
Fig. 1 is embodiment 1 a single-stage rectifying waste expansion circulation nitrogen producing craft schema;
Fig. 2 is embodiment 2 supercharging air single-stage rectifying waste expansion circulation nitrogen producing craft schemas;
Fig. 3 is embodiment 3 nitrogen supercharging single-stage rectifying waste expansion circulation nitrogen producing craft schemas.
Embodiment
Below with specific embodiment technical scheme of the present invention is described, but protection scope of the present invention is not limited thereto:
Embodiment 1
It is 600Kpa (gauge pressure is all represented with gauge pressure with overdraft) that this routine nitrogen product requires pressure.
In conjunction with Fig. 1, raw air is removed koniology and impurity through air filter 1, be compressed to 670KPa by air 2 then after, again after chilldown system 3 reduces ATs, get into purification system 4 after separating free-water, remove H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes is carried out heat exchange and is cooled to temperature of saturation through main heat exchanger 5 and expansion waste gas and nitrogen, gets into rectifying tower 6 bottoms and participates in rectifying.Obtain high pure nitrogen at rectifying tower 6 tops, the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower flows into condenser/evaporator and nitrogen phase-change heat-exchange through supercooler 7 deutomerite, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower 6 and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler 7, main heat exchanger 5 re-heats, is gone turbo-expander 8 to expand, mend to device to increase cold, expansion waste gas through supercooler 7, main heat exchanger 5 re-heats to normal temperature; Part is as the purification system resurgent gases, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower 6 tops, sees off to normal temperature through main heat exchanger 5 re-heats, and pressure is 600KPa.Said rectifying tower 6 is the sieve plate rectifying tower.
The nitrogen extraction yield is 53%, and energy consumption is 0.27 kWh/Nm
3N
2
It is 600KPa that this routine nitrogen product requires pressure.
In conjunction with Fig. 2, raw air is removed koniology and impurity through air filter 1, be compressed to 560KPa by air 2 then after, again after chilldown system 3 reduces ATs, get into purification system 4 after separating free-water, remove H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes gets into the pressurized end of booster expansion turbine group, and pressurize carries out heat exchange and is cooled to temperature of saturation through main heat exchanger 5 and expansion waste gas and nitrogen to 637KPa, gets into rectifying tower 6 bottoms and participates in rectifying.Rectifying tower 6 adopts regular packed tower (70 of number of theoretical plates, corresponding filler 100 dishes), obtains high pure nitrogen at rectifying tower 6 tops, and the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower flows into condenser/evaporator and nitrogen phase-change heat-exchange through supercooler 7 deutomerite, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower 6 and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler 7, main heat exchanger 5 re-heats, is gone turbo-expander 8 to expand, mend to device to increase cold, expansion waste gas through supercooler 7, main heat exchanger 5 re-heats to normal temperature; Part is as the purification system resurgent gases, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower 6 tops, sees off to normal temperature through main heat exchanger 5 re-heats, and pressure is 600KPa.
The nitrogen extraction yield is 60%, and energy consumption is 0.22kwh/Nm
3N
2
It is 600KPa that this routine nitrogen product requires pressure.
In conjunction with Fig. 3, raw air is removed koniology and impurity through air filter 1, be compressed to 460Kpa by air 2 then after, again after chilldown system 3 reduces ATs, get into purification system 4 after separating free-water, remove H
2O, CO
2, C
2H
2And other hydrocarbon polymer.Cleaned air passes is carried out heat exchange and is cooled to temperature of saturation through main heat exchanger 5 and expansion waste gas and nitrogen, gets into rectifying tower 6 bottoms and participates in rectifying.Rectifying tower 6 adopts regular packed tower (70 corresponding filler 100 dishes of number of theoretical plate).Obtain high pure nitrogen at rectifying tower 6 tops, the bottom obtains oxygen-enriched liquid air.Oxygen enrichment at the bottom of the tower flows into condenser/evaporator and nitrogen phase-change heat-exchange through supercooler 7 deutomerite, and nitrogen is condensed into liquid nitrogen, and major part is returned rectifying tower 6 and participated in rectifying as the phegma of tower, and small portion is seen off as liquid nitrogen product.Liquid air is evaporated as waste gas; Waste gas is drawn by the condenser/evaporator top and after supercooler 7, main heat exchanger 5 re-heats, is gone turbo-expander 8 to expand, mend to device to increase cold, expansion waste gas through supercooler 7, main heat exchanger 5 re-heats to normal temperature; Part is as the purification system resurgent gases, and all the other diffuse.Product nitrogen gas is drawn from rectifying tower 6 tops, gets into the pressurized end of booster expansion turbine group through main heat exchanger 5 re-heats to normal temperature, and pressurize send the user to 600KPa.
The nitrogen extraction yield is 64%, and energy consumption is 0.21kwh/Nm
3N
2
Claims (10)
1. a nitrogen reparation technology comprises removal of impurities, compression, precooling, the purification of air successively, it is characterized in that, rectifying was carried out in entering rectifying tower bottom after cleaned air passes was cooled to temperature of saturation, obtained nitrogen at the rectifying tower top.
2. nitrogen reparation technology as claimed in claim 1; It is characterized in that;, the oxygen-enriched liquid air that rectifier bottoms obtains gets into the condenser/evaporator and the nitrogen phase-change heat-exchange of rectifying tower top portion after the rectifying after passing through cold throttling; The liquid nitrogen that condensation obtains partly returns rectifying tower as phegma, and part is seen off as liquid nitrogen product.
3. nitrogen reparation technology as claimed in claim 2 is characterized in that, through supercooler, main heat exchanger re-heat, goes turbo-expander to expand afterwards after drawing from condenser/evaporator as waste gas with the air behind the nitrogen phase-change heat-exchange.
4. nitrogen reparation technology as claimed in claim 3 is characterized in that, the back waste gas that expands gets into main heat exchanger and cleaned air passes heat exchange, and the heat exchange rear section is as the purification system resurgent gases.
5. nitrogen reparation technology as claimed in claim 1 is characterized in that, the nitrogen that the rectifying tower top obtains goes out that rectifying tower is laggard delivers to the user after going into main heat exchanger re-heat to normal temperature.
6. like the described nitrogen reparation technology of one of claim 1-5, it is characterized in that adopting theoretical plate number is that the structured packing rectifying tower that 60-90 or corresponding filler 60-120 coil carries out rectifying.
7. nitrogen reparation technology as claimed in claim 6 is characterized in that, is compressed to after the air removal of impurities than the low 40-100Kpa of product nitrogen gas requirement pressure; Before cleaned air passes entering main heat exchanger was cooled, supercharging once more was to requiring the high 30-40Kpa of pressure than product nitrogen gas.
8. nitrogen reparation technology as claimed in claim 7 is characterized in that, the pressurized end that cleaned air passes gets into the booster expansion turbine group carries out supercharging.
9. nitrogen reparation technology as claimed in claim 6 is characterized in that, is compressed to after the air removal of impurities than the low 100-180Kpa of product nitrogen gas requirement pressure; The nitrogen that the rectifying tower top obtains goes out that rectifying tower is laggard to be gone into to be pressurized to product nitrogen gas behind main heat exchanger re-heat to the normal temperature and to require pressure to deliver to the user.
10. nitrogen reparation technology as claimed in claim 9 is characterized in that, the nitrogen that the rectifying tower top obtains goes out rectifying tower and carries out supercharging after get into the pressurized end of booster expansion turbine group behind main heat exchange re-heat to the normal temperature.
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| CN201110252527A CN102320581A (en) | 2011-08-30 | 2011-08-30 | A kind of nitrogen reparation technology |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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Address after: 475004 No. 33 Songcheng Avenue, Kaifeng City, Henan Province Applicant after: Kaifeng Huanghe Air Separation Group Co., Ltd. Address before: 475000 No. 33 Songcheng Avenue, Kaifeng economic and Technological Development Zone, Henan, China Applicant before: Kaifeng Huanghe Air Separation Group Co., Ltd. |
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Application publication date: 20120118 |