CN102538397A - Process for making nitrogen by air separation or making nitrogen and simultaneously producing oxygen in attached manner - Google Patents
Process for making nitrogen by air separation or making nitrogen and simultaneously producing oxygen in attached manner Download PDFInfo
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- CN102538397A CN102538397A CN2012100148777A CN201210014877A CN102538397A CN 102538397 A CN102538397 A CN 102538397A CN 2012100148777 A CN2012100148777 A CN 2012100148777A CN 201210014877 A CN201210014877 A CN 201210014877A CN 102538397 A CN102538397 A CN 102538397A
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- nitrogen
- oxygen
- 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
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- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention belongs to the technical field of air separation and particularly relates to a process for making nitrogen by air separation or making nitrogen and simultaneously producing oxygen in an attached manner. The process comprises the following steps of: cooling purified air and introducing into a distillation system, wherein the distillation system at least is a secondary distillation system composed of an upper distillation tower and a lower distillation tower connected into a whole by a condensate evaporator; dividing the purified air into two paths, wherein one path is to introduce the purified air into an expander for expansion refrigeration and introducing expanded air into the middle part of the upper distillation tower, and the other path is to introduce the purified air into the lower distillation tower for distillation after the purified air is cooled to the saturation temperature; and finally obtaining a nitrogen product at the top part of the upper distillation tower. The process has the beneficial effects that an air compressor is low in exhaust pressure and low in energy consumption, so that the energy consumption requirements of a nitrogen production device by air separation are greatly reduced; the current requirements of energy conservation and emission reduction in China on high energy consuming industries are satisfied; and meanwhile, the extraction rate of the nitrogen can be up to 85-97%, and the energy consumption is 0.1-0.18 kWh/Nm3N2.
Description
Technical field
The invention belongs to the air separation technology field, particularly a kind ofly produce nitrogen or nitrogen by air separation and attach the technology of producing oxygen.
Background technology
Along with The development in society and economy, in recent years, the application of high-purity nitrogen plant is constantly expanded, and all has like industries such as petrochemical industry, glass, rubber, building board, polysilicon, carbon fibers to set foot in.Industry is ever-increasing to the demand of nitrogen and oxygen, 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 makes full use of air simultaneously as far as possible, extracts wherein nitrogen and oxygen simultaneously.
Summary of the invention
The object of the present invention is to provide and a kind ofly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously, overcome that present handicraft product recovery rate is low, the bigger defective of device operation energy consumption by air separation.
The technical scheme that the present invention adopts is following:
A kind ofly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously by air separation; Cleaned air passes cooling is got into distillation system, and described distillation system is at least the two-stage rectification system that the last rectifying column that connected as one by condenser/evaporator and following rectifying column constitute; Wherein cleaned air passes is divided into two-way: wherein one the tunnel get into decompressor and carry out swell refrigeration, the back air that expands gets into goes up the rectifying column middle part, and other one the tunnel is cooled to and gets into down after the saturation temperature that rectifying column carries out rectifying; Finally, obtain product nitrogen gas at last rectifying column top.
If when only producing nitrogen by air separation, the air that rectifying column carries out rectifying under getting into obtains nitrogen at following rectifying column top, obtains oxygen-enriched liquid air in the bottom; The nitrogen that following rectifying column top obtains; In the entering condenser/evaporator of rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1, A2 or A1, A2 and A3 three parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation; The oxygen-enriched liquid air that produces in following rectifier bottoms is crossed cold deutomerite through subcooler and is flowed into the rectifying column middle part and carry out rectifying; The nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature.
A2 partly gets into down the top of rectifying column as phegma, and A3 partly crosses cold back through subcooler and takes out as nitrogen products.
The waste gas that last rectifying column bottom produces after subcooler and main heat exchanger re-heat as the purification system regeneration gas.
If producing nitrogen by air separation attaches when producing oxygen simultaneously; Described distillation system is three grades of distillation systems; Described three grades of distillation systems by the two-stage rectification system and the oxygen column after being connected in the two-stage rectification system constitute; After the rectifying, obtain product nitrogen gas, obtain product oxygen or liquid oxygen in the oxygen column bottom at last rectifying column top.
An air part that is cooled to saturation temperature after the purification gets into down that rectifying column carries out outside the rectifying, the evaporimeter that remainder gets into the oxygen column bottom as thermal source and the middle part that in evaporimeter, got into rectifying column by the liquid oxygen cooling of oxygen column bottom as phegma.
The air that rectifying column carries out rectifying under getting into obtains nitrogen at following rectifying column top, obtains oxygen-enriched liquid air in the bottom; The nitrogen that following rectifying column top obtains; In the entering condenser/evaporator of rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1, A2 two parts or A1, A2 and A3 three parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation; The oxygen-enriched liquid air that produces in following rectifier bottoms is crossed cold deutomerite through subcooler and is flowed into the rectifying column middle part and carry out rectifying; The nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature; The oxygen-enriched liquid air throttling that produces in last rectifier bottoms gets into the oxygen column top as the oxygen column phegma, obtains oxygen or liquid oxygen product in the oxygen column bottom.
A2 partly gets into down the top of rectifying column as phegma, and A3 partly crosses cold back through subcooler and takes out as nitrogen products.
Wherein A3 part can be told and also can not tell but directly only be divided into A1 and A2, when being divided into two parts, can obtain nitrogen and oxygen, when being divided into three parts, can also obtain liquid nitrogen product.
The emptying or as the purification system regeneration gas after the main heat exchanger re-heat of oxygen column top waste gas, the waste gas that last rectifying column bottom produces after subcooler and main heat exchanger re-heat as the purification system regeneration gas.
In the above-mentioned technology, raw air is compressed to 0.35～0.45MPa (G) by air compressor after removal of impurities, and precooling to air themperature is 5-12 ℃ again, gets into purification system then and purifies.
When carrying out swell refrigeration, cleaned air passes can adopt the turbine boosting unit that expands.
In the described two-stage rectification system, last rectifying column can adopt the structured packing rectifying column of structured packing 50-120 dish to carry out rectifying.
Be back at last that oxygen content is about 50～90% in the regeneration gas of purification system, regeneration temperature is 145-155 ℃.
The row pressure of this technology air compressor is low, is about 0.35-0.45Mpa; The nitrogen recovery rate is 85～97%, can produce 1～2% liquid nitrogen and/or liquid oxygen (both sums are 1-2%) simultaneously, and energy consumption is 0.1-0.18 kWh/Nm
3N
2
Below set forth technology of the present invention from another angle again:
Raw air is removed dust in air and impurity through air cleaner, is compressed to 0.35～0.45MPa (G) by air compressor then, and reducing air themperature through chilldown system again is 5-12 ℃, gets into purification system after separating free water, removes H
2O, CO
2, C
2H
2And other hydrocarbon.
When 1) only producing nitrogen: cleaned air passes is divided into two-way: wherein part air entering decompressor carries out swell refrigeration; The back air that expands is participated in rectifying in the middle part of getting into and going up rectifying column; The following rectifying column of entering carried out rectifying after remaining air was cooled to saturation temperature; Obtain nitrogen at following rectifying column top, obtain oxygen-enriched liquid air in the bottom.
2) produce the technology of nitrogen and oxygen simultaneously: cleaned air passes is divided into two-way: wherein the part air gets into decompressor and carries out swell refrigeration; The back air that expands is participated in rectifying in the middle part of getting into and going up rectifying column; Remaining air is cooled to and is divided into B, C two parts after the saturation temperature: wherein B partly gets into down the rectifying column bottom and carries out rectifying; Obtain nitrogen at following rectifying column top, obtain oxygen-enriched liquid air in the bottom; C part air gets into the liquid oxygen phase-change heat-exchange of the evaporimeter of oxygen column bottom as thermal source and oxygen column bottom.
Common ground: the condenser/evaporator that the nitrogen that following rectifying column top obtains go into to be gone up the rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1, A2 or A1, A2 and A3 three parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation.A2 partly gets into down the top of rectifying column as phegma, and A3 partly crosses cold back through subcooler and takes out as nitrogen products.The oxygen-enriched liquid air that produces in following rectifier bottoms is crossed cold deutomerite through subcooler and is flowed into the rectifying column middle part and carry out rectifying.Obtain at last rectifying column top nitrogen after subcooler and main heat exchanger re-heat as product nitrogen gas.Waste gas (50～90% O that last rectifying column bottom produces
2) after subcooler and main heat exchanger re-heat as the purification system regeneration gas, regeneration temperature is 145-155 ℃.
When 1) only producing nitrogen, so far promptly accomplish the flow process of whole technology.
2) produce the technology of nitrogen and oxygen simultaneously: the evaporimeter that C part air gets into the oxygen column bottom as the liquid oxygen phase-change heat-exchange of thermal source bottom oxygen column after; The middle part that rectifying column is gone up in air setting throttling entering is as phegma, and the oxygen-enriched liquid air throttling that produces in last rectifier bottoms gets into the oxygen column top as the oxygen column phegma; The liquid oxygen evaporation is as the rising steam of oxygen column.Obtain oxygen or liquid oxygen product at last in the oxygen column bottom; And the emptying or as the purification system regeneration gas after the main heat exchanger re-heat of oxygen column top waste gas.So far also accomplish the flow process of whole technology.
In the above-mentioned technology, concrete reflux ratio and other each parameters can be adjusted according to the situation of concrete rectifying column and oxygen column by those skilled in the art, also can assist means such as existing simulation softward, set forth no longer one by one here.
The present invention has following advantage with respect to prior art:
Nitrogen reparation technology air compressor of the present invention row pressure low (0.35-0.45Mpa); Energy consumption is low; Greatly reduce the energy consumption requirement of nitrogen production by air separation device; Meet the requirement of the present energy-saving and emission-reduction to high energy-consuming industry of country, the nitrogen recovery rate can reach 85-97% simultaneously, and energy consumption is 0.1-0.18 kWh/Nm
3N
2
Description of drawings
Fig. 1 is only produced the process chart of nitrogen by air separation for embodiment 1;
Fig. 2 produces the nitrogen also process chart of by-product oxygen simultaneously for embodiment 2 by air separation.
The specific embodiment
Below with specific embodiment technical scheme of the present invention is described, but protection scope of the present invention is not limited thereto:
Produce nitrogen 30500 Nm
3/ h
In conjunction with Fig. 1, raw air 43000 Nm
3/ h removes dust in air and impurity through air cleaner 1, be compressed to 0.41MPa by air compressor 2 then after, reduce air themperatures to 5-8 ℃ through chilldown system 3 again, get into purification system 4 after separating free water, remove H
2O, CO
2, C
2H
2And other hydrocarbon.
Cleaned air passes is divided into two-way: 9500 Nm wherein
3The air of/h gets into booster expansion machine 5 and carries out swell refrigeration; The back air that expands gets into goes up the participation rectifying of rectifying column 6 middle parts; The following rectifying column 7 of entering carried out rectifying after remaining air was cooled to saturation temperature, obtained nitrogen at following rectifying column 7 tops, obtained oxygen-enriched liquid air in the bottom.
The condenser/evaporator that the nitrogen that following rectifying column 7 tops obtain go into to be gone up rectifying column 6 bottoms as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifying column 6 bottoms be cooled to liquid nitrogen, be divided into three parts, wherein 14300 Nm
3The liquid nitrogen of/h is crossed cold deutomerite through subcooler 8 and is flowed into rectifying column 6 tops as upward tower (adopting the structured packing of corresponding filler 60 dishes) rectifying of phegma participation.
20000 Nm
3The liquid nitrogen of/h gets into the top of following rectifying column 7 as phegma, 650 Nm
3The liquid nitrogen of/h is crossed cold back through subcooler 8 and is taken out as nitrogen products.
Cross cold deutomerite at the oxygen-enriched liquid air of rectifying column 7 bottoms generation down through subcooler 8 and flow into rectifying column 6 middle parts.Obtain 30500 Nm at last rectifying column 6 tops
3/ h nitrogen after subcooler 8 and main heat exchanger 9 re-heats as product nitrogen gas, 11000 Nm that the bottom produces
3/ h waste gas (78% O
2) after subcooler 8 and main heat exchanger 9 re-heats as purification system 4 regeneration gases, regeneration temperature is 150 ℃.
The nitrogen recovery rate is 95%, and energy consumption is 0.12 kWh/Nm
3N
2
Embodiment 2
Produce nitrogen: 25000 Nm
3/ h, liquid oxygen: 500 Nm
3/ h.
In conjunction with Fig. 2, raw air 34000 Nm
3/ h removes dust in air and impurity through air cleaner 1, be compressed to 0.41MPa by air compressor 2 then after, reduce air themperatures to 5-8 ℃ through chilldown system 3 again, get into purification system 4 after separating free water, remove H
2O, CO
2, C
2H
2And other hydrocarbon.
Cleaned air passes is divided into two-way: 9000 Nm wherein
3The air of/h gets into decompressor 5 and carries out swell refrigeration, and the back air that expands gets into to be gone up rectifying column 6 (adopting the structured packing of corresponding filler 60 dishes) middle part and participate in rectifying, and remaining air is cooled to separated into two parts after the saturation temperature: 23700 Nm wherein
3The air of/h gets into down, and rectifying column 7 obtains 25000 Nm as rising steam participation rectifying through being separated in down rectifying column 7 tops
3The nitrogen of/h, in the entering condenser/evaporator of rectifying column 6 bottoms as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifying column 6 bottoms be cooled to liquid nitrogen, be divided into two parts, wherein 11000 Nm
3/ h liquid nitrogen is crossed cold deutomerite through subcooler 8 and is flowed into rectifying column 6 tops as upward tower rectifying of phegma participation, 14000 Nm
3The top of rectifying column 7 was as phegma under/h liquid nitrogen got into.
Cross cold deutomerite at the oxygen-enriched liquid air of rectifying column 7 bottoms generation down through subcooler 8 and flow into rectifying column 6 middle parts.Obtain 25000 Nm at last rectifying column 6 tops
3/ h nitrogen after subcooler 8 and main heat exchanger 9 re-heats as product nitrogen gas, 7400 Nm that the bottom produces
3/ h waste gas (77% O
2) as purification system 4 regeneration gases, regeneration temperature is 150 ℃ to waste gas after subcooler 8 and main heat exchanger 9 re-heats.
Be cooled to other 1300 Nm after the saturation temperature
3The evaporimeter that/h air gets into oxygen column 10 bottoms as thermal source and the middle part that in evaporimeter, got into rectifying column 6 by the cooling of the liquid oxygen of oxygen column 10 bottoms as phegma.Oxygen-enriched liquid air (91% O that produces in last rectifying column 6 bottoms
2) get into oxygen column 10 tops as oxygen column 10 phegmas.Oxygen column 10 tops 1000 Nm
3The emptying or as the purification system regeneration gas, the bottom obtains 500 Nm after main heat exchanger 9 re-heats of/h waste gas
3/ h liquid oxygen product.
The nitrogen recovery rate is 96%, and energy consumption is 0.13 kWh/Nm
3N
2
The foregoing description is the preferred embodiment of the present invention, but embodiment of the present invention is not restricted to the described embodiments, and other the change that any the present invention of not deviating from did all should be the substitute mode of equivalence, is included within protection scope of the present invention.
Claims (10)
1. produce nitrogen by air separation or produce nitrogen and attach the technology of producing oxygen simultaneously for one kind; It is characterized in that; Cleaned air passes cooling is got into distillation system, and described distillation system is at least the two-stage rectification system that the last rectifying column that connected as one by condenser/evaporator and following rectifying column constitute; Wherein cleaned air passes is divided into two-way: wherein one the tunnel get into decompressor and carry out swell refrigeration, the back air that expands gets into goes up the rectifying column middle part, and other one the tunnel is cooled to and gets into down after the saturation temperature that rectifying column carries out rectifying; Finally, obtain product nitrogen gas at last rectifying column top.
2. as claimed in claim 1ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously by air separation; It is characterized in that, when only producing nitrogen by air separation, the air that rectifying column carries out rectifying under getting into; Obtain nitrogen at following rectifying column top, obtain oxygen-enriched liquid air in the bottom; The nitrogen that following rectifying column top obtains; In the entering condenser/evaporator of rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1, A2 two parts or A1, A2 and A3 three parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation; The oxygen-enriched liquid air that produces in following rectifier bottoms is crossed cold deutomerite through subcooler and is flowed into the rectifying column middle part and carry out rectifying; The nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature.
3. as claimed in claim 2ly produced nitrogen or produced nitrogen and attach the technology of producing oxygen simultaneously by air separation, it is characterized in that A2 partly gets into down the top of rectifying column as phegma, A3 partly crosses the taking-up of cold back as nitrogen products through subcooler.
4. as claimed in claim 3ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously, it is characterized in that by air separation, the waste gas of last rectifying column bottom generation after subcooler and main heat exchanger re-heat as the purification system regeneration gas.
5. as claimed in claim 1ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously by air separation; It is characterized in that produce nitrogen by air separation and attach simultaneously when producing oxygen, described distillation system is three grades of distillation systems; Described three grades of distillation systems by the two-stage rectification system and the oxygen column after being connected in the two-stage rectification system constitute; After the rectifying, obtain product nitrogen gas, obtain product oxygen or liquid oxygen in the oxygen column bottom at last rectifying column top.
6. as claimed in claim 5ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously by air separation; It is characterized in that; An air part that is cooled to saturation temperature after the purification gets into down that rectifying column carries out outside the rectifying, the evaporimeter that remainder gets into the oxygen column bottom as thermal source and the middle part that in evaporimeter, got into rectifying column by the liquid oxygen cooling of oxygen column bottom as phegma.
7. as claimed in claim 6ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously, it is characterized in that, get into the air that rectifying column down carries out rectifying, obtain nitrogen, obtain oxygen-enriched liquid air in the bottom at rectifying column top down by air separation; The nitrogen that following rectifying column top obtains; In the entering condenser/evaporator of rectifying column bottom as thermal source and in condenser/evaporator by on the oxygen-enriched liquid air of rectifier bottoms be cooled to liquid nitrogen; Be divided into A1, A2 or A1, A2 and A3 three parts simultaneously, wherein the A1 part liquid nitrogen is crossed cold deutomerite through subcooler and is flowed into the rectifying column top as upward tower rectifying of phegma participation; The oxygen-enriched liquid air that produces in following rectifier bottoms is crossed cold deutomerite through subcooler and is flowed into the rectifying column middle part and carry out rectifying; The nitrogen at last rectifying column top goes out tower after deliver to the user as nitrogen product behind subcooler and main heat exchanger re-heat to the normal temperature; The oxygen-enriched liquid air throttling that produces in last rectifier bottoms gets into the oxygen column top as the oxygen column phegma, obtains oxygen or liquid oxygen product in the oxygen column bottom.
8. as claimed in claim 7ly produced nitrogen or produced nitrogen and attach the technology of producing oxygen simultaneously by air separation, it is characterized in that A2 partly gets into down the top of rectifying column as phegma, A3 partly crosses the taking-up of cold back as nitrogen products through subcooler; The emptying or as the purification system regeneration gas after the main heat exchanger re-heat of oxygen column top waste gas, the waste gas that last rectifying column bottom produces after subcooler and main heat exchanger re-heat as the purification system regeneration gas.
9. produce nitrogen or produce the technology that nitrogen attaches product oxygen simultaneously by air separation as one of claim 1-8 is described; It is characterized in that; Raw air is compressed to 0.35～0.45MPa (G) by air compressor after removal of impurities; Precooling to air themperature is 5-12 ℃ again, gets into purification system then and purifies.
10. as claimed in claim 9ly produce nitrogen or produce nitrogen and attach the technology of producing oxygen simultaneously, it is characterized in that the structured packing rectifying column of last rectifying column for adopting structured packing 50-120 to coil by air separation.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103148677A (en) * | 2013-01-27 | 2013-06-12 | 南京瑞柯徕姆环保科技有限公司 | Air separation system for isobarically separating oxygen and nitrogen from air |
| CN103438663A (en) * | 2013-07-11 | 2013-12-11 | 开封黄河空分集团有限公司 | Device and process for preparing high-purity oxygen and nitrogen under ultra-low pressure |
| CN104061757A (en) * | 2014-07-07 | 2014-09-24 | 开封空分集团有限公司 | Liquid oxygen and liquid nitrogen preparation device and method |
| CN106595221A (en) * | 2015-10-20 | 2017-04-26 | 乔治洛德方法研究和开发液化空气有限公司 | Oxygen production system and oxygen production method |
| CN113566495A (en) * | 2021-07-28 | 2021-10-29 | 杭州特盈能源技术发展有限公司 | Low-energy-consumption nitrogen and oxygen preparation process for glass kiln |
| CN113883829A (en) * | 2021-11-01 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Method for preparing high-purity nitrogen with low energy consumption and method for preparing high-purity nitrogen with low energy consumption |
| CN114130153A (en) * | 2021-11-20 | 2022-03-04 | 开封黄河空分集团有限公司 | Air separation device and method for preparing large liquid amount |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058644A (en) * | 1990-06-27 | 1992-02-12 | 联合碳化工业气体技术公司 | Cryognic air separation system with dual product side condenser |
| CN1080990A (en) * | 1992-06-01 | 1994-01-19 | 普拉塞尔技术有限公司 | Auxiliary column cryogenic rectification system |
| CN1098194A (en) * | 1993-05-13 | 1995-02-01 | 普拉塞尔技术有限公司 | A kind of low temperature distillation system that has the liquid oxygen evaporimeter |
| US5463871A (en) * | 1994-10-04 | 1995-11-07 | Praxair Technology, Inc. | Side column cryogenic rectification system for producing lower purity oxygen |
| US6626008B1 (en) * | 2002-12-11 | 2003-09-30 | Praxair Technology, Inc. | Cold compression cryogenic rectification system for producing low purity oxygen |
| CN102003867A (en) * | 2010-11-09 | 2011-04-06 | 上海启元科技发展有限公司 | Method for producing high-purity nitrogen and low-purity oxygen |
| CN102213537A (en) * | 2011-04-18 | 2011-10-12 | 开封黄河空分集团有限公司 | Separation technique for low pressure oxygen-enriched air |
-
2012
- 2012-01-18 CN CN2012100148777A patent/CN102538397A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1058644A (en) * | 1990-06-27 | 1992-02-12 | 联合碳化工业气体技术公司 | Cryognic air separation system with dual product side condenser |
| CN1080990A (en) * | 1992-06-01 | 1994-01-19 | 普拉塞尔技术有限公司 | Auxiliary column cryogenic rectification system |
| CN1098194A (en) * | 1993-05-13 | 1995-02-01 | 普拉塞尔技术有限公司 | A kind of low temperature distillation system that has the liquid oxygen evaporimeter |
| US5463871A (en) * | 1994-10-04 | 1995-11-07 | Praxair Technology, Inc. | Side column cryogenic rectification system for producing lower purity oxygen |
| US6626008B1 (en) * | 2002-12-11 | 2003-09-30 | Praxair Technology, Inc. | Cold compression cryogenic rectification system for producing low purity oxygen |
| CN102003867A (en) * | 2010-11-09 | 2011-04-06 | 上海启元科技发展有限公司 | Method for producing high-purity nitrogen and low-purity oxygen |
| CN102213537A (en) * | 2011-04-18 | 2011-10-12 | 开封黄河空分集团有限公司 | Separation technique for low pressure oxygen-enriched air |
Non-Patent Citations (1)
| Title |
|---|
| 李化治: "《制氧技术》", 31 December 2009, article "筛板塔、填料塔", pages: 186-207 * |
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| CN103148677B (en) * | 2013-01-27 | 2015-06-10 | 南京瑞柯徕姆环保科技有限公司 | Air separation system for isobarically separating oxygen and nitrogen from air |
| CN103438663A (en) * | 2013-07-11 | 2013-12-11 | 开封黄河空分集团有限公司 | Device and process for preparing high-purity oxygen and nitrogen under ultra-low pressure |
| CN104061757A (en) * | 2014-07-07 | 2014-09-24 | 开封空分集团有限公司 | Liquid oxygen and liquid nitrogen preparation device and method |
| CN104061757B (en) * | 2014-07-07 | 2016-09-07 | 开封空分集团有限公司 | A kind of liquid oxygen and liquid nitrogen device for making and method |
| CN106595221A (en) * | 2015-10-20 | 2017-04-26 | 乔治洛德方法研究和开发液化空气有限公司 | Oxygen production system and oxygen production method |
| CN113566495A (en) * | 2021-07-28 | 2021-10-29 | 杭州特盈能源技术发展有限公司 | Low-energy-consumption nitrogen and oxygen preparation process for glass kiln |
| US11629914B2 (en) | 2021-07-28 | 2023-04-18 | Hangzhou Turning Energy Technology Development Co., Ltd. | Energy-efficient process for preparing nitrogen and oxygen for glass melting furnace |
| CN113883829A (en) * | 2021-11-01 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Method for preparing high-purity nitrogen with low energy consumption and method for preparing high-purity nitrogen with low energy consumption |
| CN113883829B (en) * | 2021-11-01 | 2023-02-28 | 四川空分设备(集团)有限责任公司 | Method and device for preparing high-purity nitrogen with low energy consumption |
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