CN102213537A - Separation technique for low pressure oxygen-enriched air - Google Patents
Separation technique for low pressure oxygen-enriched air Download PDFInfo
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- CN102213537A CN102213537A CN201110096197XA CN201110096197A CN102213537A CN 102213537 A CN102213537 A CN 102213537A CN 201110096197X A CN201110096197X A CN 201110096197XA CN 201110096197 A CN201110096197 A CN 201110096197A CN 102213537 A CN102213537 A CN 102213537A
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Abstract
The invention belongs to the field of air separation technology and in particular relates to a separation technique for low pressure oxygen-enriched air, comprising the steps of impurity removal by means of air filtration, compression to 0.33-0.44MPa with an air compressor, purification, heat exchange, rectification, liquid oxygen vaporization and pressurization. The technique has the characteristics of being simple in technological process, convenient in operation, stable and reliable in running, stable in oxygen purity of the product, less in outside interference factors, long in continuous running period, low in power consumption for oxygen generation, low in equipment cost, high in automation degree and convenient in engine start and stop.
Description
Technical field
The invention belongs to the air separation technology field, be specifically related to a kind of low pressure oxygen-enriched air separating technology.
Background technology
Air separation is called for short empty the branch, it is the difference of utilizing each component physical property in the air, from air, isolate oxygen and nitrogen, or extract the process of rare gas such as helium, argon gas simultaneously, be widely used in industrial departments such as metallurgy, chemical industry, oil, machinery, mining, food, military affairs.
The modern air separation that realizes produces highly purified oxygen, nitrogen product, generally uses low temperature process and absorption method dual mode.By comparison, use the resulting product purity height of low temperature process, oxygen purity can reach more than 99.6%, nitrogen purity can reach 99.999% especially, but the system oxygen energy consumption height of low temperature process, complicated operation, the oxygen that the user seeks out low-purity then needs to add air adjustment purity.The advantage of absorption method is that flow process is simple, and easy to operate, operating cost is lower, but system oxygen purity can only reach 93%, and can only produce a kind of product.
Summary of the invention
The object of the present invention is to provide a kind of energy-conservation low pressure oxygen-enriched air separating technology.
The present invention is by the following technical solutions:
Low pressure oxygen-enriched air separating technology the steps include: that (1) air through the filter filtering and impurity removing, enters air compressor machine and is compressed to 0.33-0.44MPa, is cooled to 5-10 ℃ then, continues to be fed into molecular sieve adsorber and purifies; (2) cleaned air passes is divided two-way, one the tunnel enters the empty expansion gas passage that divides the fractionating column main heat exchanger as expanded air, extract out by the main heat exchanger middle part then and enter the decompressor expansion, another road air directly is cooled to dew-point temperature through main heat exchanger, continuation is through dividing tower rectifying under the fractionating column through entering sky behind the oxygen evaporator again, tower bottom obtains oxygen-enriched liquid air under the empty branch fractionating column, and top of tower obtains nitrogen under the empty branch fractionating column; (3) air crossed after expanding with decompressor in cold back of the empty oxygen-enriched liquid air that divides tower bottom under the fractionating column enters the empty tower rectifying on the fractionating column that divides, and emptyly divides that top of tower obtains nitrogen on the fractionating column; (4) emptyly divide tower bottom obtains on the fractionating column liquid oxygen to enter oxygen evaporator to be vaporized from the air heat of main heat exchanger, oxygen pressure is increased to 65-80KPa, and supercharging obtains oxygen product after the main heat exchanger re-heat.
Described liquid oxygen evaporimeter comprises shell, be provided with plate-fin heat exchanger in the shell, plate-fin heat exchanger comprises at least one plate fin heat-exchanging unit, the plate fin heat-exchanging unit comprises oxygen channel and the air duct that is crisscross arranged, wherein, oxygen channel is a straight channel, air duct is a wing passage, oxygen channel and air duct are respectively by between adjacent two dividing plates fin being set, flow deflector and strip of paper used for sealing are formed, the import department of described air duct and exit are respectively equipped with end socket and adapter, adapter extends to outside the shell, and the sidewall of shell is provided with the liquid oxygen inlet pipe, and cover top portion is provided with oxygen and goes out pipe.
The bottom of described shell is provided with base.
The used fin of described air duct is a serrated fin, and flow deflector is straight perforated fin; The used fin of described oxygen channel is straight perforated fin, and flow deflector is straight perforated fin.
The oxygen purity 80-95% that low pressure oxygen-enriched air separating technology of the present invention obtains, oxygen recovery rate 99.8%, pneumatics unit pressure at expulsion 0.33-0.44MPa, system of unit oxygen air separation power consumption 0.367-0.425 kwh/Nm
3O
2(amount to 99.6% O
2), the pneumatics unit pressure at expulsion 0.52-0.62 in compared to existing technology
MPa greatly reduces the air compressor machine energy consumption, can contribute for national energy-saving and emission-reduction strategy.Bring up to 65-80Kpa by 20 original Kpa before entering the oxygen compressor group after the oxygen re-heat, oxygen compressor group pressure ratio is significantly reduced, make the oxygen compressor operation more stable, easily worn part is longer running time, changes number of times and reduces, and maintenance cost descends, the reduction of oxygen compressor pressure ratio directly causes the decline of shaft power, press the oxygen power consumption to decline to a great extent, energy efficient is saved resource.
The liquid oxygen that tower bottom obtains on the empty branch of the present invention fractionating column is entered in the shell by the liquid oxygen inlet pipe of oxygen evaporator, the liquid level of liquid oxygen rises gradually and is immersed in the oxygen channel of plate-fin heat exchanger, and simultaneously enter air duct by the air inlet pipe from the air of main heat exchanger, it is oxygen that thereby air in the air duct and the liquid oxygen heat exchange in the oxygen channel make vaporization of liquid oxygen, realizes the liquid oxygen evaporation.
Technological process of the present invention is simple, and is easy to operate, stable and reliable operation, and the product oxygen purity is stable, and it is few to be subjected to the external interference factor, and the continuous cycle of operation is long, and system oxygen power consumption is low, equipment investment is few; Operation automaticity height, the start-stop car is convenient.
Description of drawings
Fig. 1 is the structural representation of oxygen evaporator among the present invention;
Fig. 2 is the A-A view of Fig. 1;
Fig. 3 is the structural representation of the inner plate-fin heat exchange unit of oxygen evaporator;
Fig. 4 is the structural representation of the inner plate-fin heat exchange unit of oxygen evaporator.
The specific embodiment
Embodiment 1
Low pressure oxygen-enriched air separating technology the steps include: that (1) air removes by filter dust and mechanical admixture through filter, enters air compressor machine and is compressed to 0.33MPa, is cooled to 5 ℃ then, continues to be fed into molecular sieve adsorber and purifies; (2) cleaned air passes is divided two-way, one the tunnel enters the empty expansion gas passage that divides the fractionating column main heat exchanger as expanded air, extract out by the main heat exchanger middle part then and enter the decompressor expansion, another road air is cooled to dew-point temperature after oxygen evaporator enters the empty tower rectifying under the fractionating column that divides, tower bottom obtains oxygen-enriched liquid air under the empty branch fractionating column, and top of tower obtains nitrogen under the empty branch fractionating column; (3) air crossed after expanding with decompressor in cold back of the empty oxygen-enriched liquid air that divides tower bottom under the fractionating column enters the empty tower rectifying on the fractionating column that divides, and emptyly divides that top of tower obtains nitrogen on the fractionating column; (4) emptyly divide tower bottom obtains on the fractionating column liquid oxygen to enter oxygen evaporator to be vaporized from the air heat of main heat exchanger, oxygen pressure is increased to 65KPa, and to obtain purity be 80%O after the oxygen compressor group is pressurized to 0.2MPa through the main heat exchanger re-heat
2
Oxygen evaporator such as Fig. 1,2,3, shown in 4, comprise shell 1, the bottom of shell 1 is provided with base 5, be provided with plate-fin heat exchanger in the shell 1, plate-fin heat exchanger comprises two plate fin heat-exchanging unit 20 that are arranged side by side, plate fin heat-exchanging unit 20 comprises oxygen channel 7 and the air duct 8 that is crisscross arranged, wherein, oxygen channel 7 is a straight channel, air duct 8 is a wing passage, oxygen channel 7 is provided with straight perforated fin 72 by 10 on adjacent two dividing plates, flow deflector 71 and strip of paper used for sealing 70 are formed, air duct 8 is provided with serrated fin 82 by 9 on adjacent two dividing plates respectively, flow deflector 81 and strip of paper used for sealing 80 are formed, the import department of air duct 8 is provided with end socket 21 and air inlet pipe 2, air inlet pipe 2 extends to outside the shell 1, and the exit of air duct 8 is provided with end socket 41 and air goes out pipe 4, and the sidewall of shell 1 is provided with liquid oxygen inlet pipe 3, shell 1 top is provided with oxygen and goes out pipe 6, flow deflector 71,81 is straight perforated fin.
Use space-time to divide the liquid oxygen that tower bottom obtains on the fractionating column to enter in the shell 1 by liquid oxygen inlet pipe 3, the liquid level of liquid oxygen rises gradually and is immersed in the oxygen channel 7 of plate fin heat-exchanging unit 20, and simultaneously enter air duct 8 by air inlet pipe 2 from the air of main heat exchanger, liquid oxygen heat exchange in air in the air duct 8 and the oxygen channel 7, the heat of vaporization boiling of liquid oxygen absorption air is vaporizated into oxygen gradually and upwards goes out pipe 6 discharges by oxygen, thus the evaporation of realization liquid oxygen.
The direction of arrow is the flow direction of material among the figure.
Low pressure oxygen-enriched air separating technology the steps include: that (1) air removes by filter dust and mechanical admixture through filter, enters air compressor machine and is compressed to 0.38MPa, is cooled to 8 ℃ then, continues to be fed into molecular sieve adsorber and purifies; (2) cleaned air passes is divided two-way, one the tunnel enters the empty expansion gas passage that divides the fractionating column main heat exchanger as expanded air, extract out by the main heat exchanger middle part then and enter the decompressor expansion, another road air is cooled to dew-point temperature after oxygen evaporator enters the empty tower rectifying under the fractionating column that divides, tower bottom obtains oxygen-enriched liquid air under the empty branch fractionating column, and top of tower obtains nitrogen under the empty branch fractionating column; (3) air crossed after expanding with decompressor in cold back of the empty oxygen-enriched liquid air that divides tower bottom under the fractionating column enters the empty tower rectifying on the fractionating column that divides, and emptyly divides that top of tower obtains nitrogen on the fractionating column; (4) emptyly divide tower bottom obtains on the fractionating column liquid oxygen to enter oxygen evaporator to be vaporized from the air heat of main heat exchanger, oxygen pressure is increased to 70KPa, and to obtain purity be 90% O after the oxygen compressor group is pressurized to 0.8MPa through the main heat exchanger re-heat
2
Liquid oxygen and air utilize the process of oxygen evaporator heat exchange with embodiment 1.
Embodiment 3
Low pressure oxygen-enriched air separating technology the steps include: that (1) air removes by filter dust and mechanical admixture through filter, enters air compressor machine and is compressed to 0.44MPa, is cooled to 10 ℃ then, continues to be fed into molecular sieve adsorber and purifies; (2) cleaned air passes is divided two-way, one the tunnel enters the empty expansion gas passage that divides the fractionating column main heat exchanger as expanded air, extract out by the main heat exchanger middle part then and enter the decompressor expansion, another road air is cooled to dew-point temperature after oxygen evaporator enters the empty tower rectifying under the fractionating column that divides, tower bottom obtains oxygen-enriched liquid air under the empty branch fractionating column, and top of tower obtains nitrogen under the empty branch fractionating column; (3) air crossed after expanding with decompressor in cold back of the empty oxygen-enriched liquid air that divides tower bottom under the fractionating column enters the empty tower rectifying on the fractionating column that divides, and emptyly divides that top of tower obtains nitrogen on the fractionating column; (4) emptyly divide tower bottom obtains on the fractionating column liquid oxygen to enter oxygen evaporator to be vaporized from the air heat of main heat exchanger, oxygen pressure is increased to 80KPa, and to obtain purity be 95% O after the oxygen compressor group is pressurized to 1.6MPa through the main heat exchanger re-heat
2
Liquid oxygen and air utilize the process of oxygen evaporator heat exchange with embodiment 1.
Claims (4)
1. low pressure oxygen-enriched air separating technology the steps include: that (1) air through the filter filtering and impurity removing, enters air compressor machine and is compressed to 0.33-0.44MPa, is cooled to 5-10 ℃ then, continues to be fed into molecular sieve adsorber and purifies; (2) cleaned air passes is divided two-way, one the tunnel enters the empty expansion gas passage that divides the fractionating column main heat exchanger as expanded air, extract out by the main heat exchanger middle part then and enter the decompressor expansion, another road air directly is cooled to dew-point temperature through main heat exchanger, continuation is through dividing tower rectifying under the fractionating column through entering sky behind the oxygen evaporator again, tower bottom obtains oxygen-enriched liquid air under the empty branch fractionating column, and top of tower obtains nitrogen under the empty branch fractionating column; (3) air crossed after expanding with decompressor in cold back of the empty oxygen-enriched liquid air that divides tower bottom under the fractionating column enters the empty tower rectifying on the fractionating column that divides, and emptyly divides that top of tower obtains nitrogen on the fractionating column; (4) emptyly divide tower bottom obtains on the fractionating column liquid oxygen to enter oxygen evaporator to be vaporized from the air heat of main heat exchanger, oxygen pressure is increased to 65-80KPa, and supercharging obtains oxygen product after the main heat exchanger re-heat.
2. low pressure oxygen-enriched air separating technology as claimed in claim 1, it is characterized in that: described liquid oxygen evaporimeter comprises shell, be provided with plate-fin heat exchanger in the shell, plate-fin heat exchanger comprises at least one plate fin heat-exchanging unit, the plate fin heat-exchanging unit comprises oxygen channel and the air duct that is crisscross arranged, wherein, oxygen channel is a straight channel, air duct is a wing passage, oxygen channel and air duct are respectively by between adjacent two dividing plates fin being set, flow deflector and strip of paper used for sealing are formed, the import department of described air duct and exit are respectively equipped with end socket and adapter, adapter extends to outside the shell, the sidewall of shell is provided with the liquid oxygen inlet pipe, and cover top portion is provided with oxygen and goes out pipe.
3. low pressure oxygen-enriched air separating technology as claimed in claim 2, it is characterized in that: the bottom of described shell is provided with base.
4. as claim 2 or 3 described low pressure oxygen-enriched air separating technologies, it is characterized in that: the used fin of described air duct is a serrated fin, and flow deflector is straight perforated fin; The used fin of described oxygen channel is straight perforated fin, and flow deflector is straight perforated fin.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110096197XA CN102213537A (en) | 2011-04-18 | 2011-04-18 | Separation technique for low pressure oxygen-enriched air |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110096197XA CN102213537A (en) | 2011-04-18 | 2011-04-18 | Separation technique for low pressure oxygen-enriched air |
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| CN102213537A true CN102213537A (en) | 2011-10-12 |
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| CN201110096197XA Pending CN102213537A (en) | 2011-04-18 | 2011-04-18 | Separation technique for low pressure oxygen-enriched air |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102538397A (en) * | 2012-01-18 | 2012-07-04 | 开封黄河空分集团有限公司 | Process for making nitrogen by air separation or making nitrogen and simultaneously producing oxygen in attached manner |
| CN106403498A (en) * | 2016-09-06 | 2017-02-15 | 广西南宁市邕检科技有限公司 | Novel rotation evaporator |
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| CN1112669A (en) * | 1994-02-08 | 1995-11-29 | 普拉塞尔技术有限公司 | Cryogenic recification system with hybrid product boiler |
| CN1119733A (en) * | 1993-08-06 | 1996-04-03 | 普拉塞尔技术有限公司 | Cryogenic rectification system for lower pressure operation |
| CN1152702A (en) * | 1995-07-21 | 1997-06-25 | 缔酸株式会社 | Method and apparatus for preparing high-purity nitrogen |
| CN1165286A (en) * | 1996-03-18 | 1997-11-19 | 波克股份有限公司 | Heat exchanger |
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2011
- 2011-04-18 CN CN201110096197XA patent/CN102213537A/en active Pending
Patent Citations (4)
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| CN1119733A (en) * | 1993-08-06 | 1996-04-03 | 普拉塞尔技术有限公司 | Cryogenic rectification system for lower pressure operation |
| CN1112669A (en) * | 1994-02-08 | 1995-11-29 | 普拉塞尔技术有限公司 | Cryogenic recification system with hybrid product boiler |
| CN1152702A (en) * | 1995-07-21 | 1997-06-25 | 缔酸株式会社 | Method and apparatus for preparing high-purity nitrogen |
| CN1165286A (en) * | 1996-03-18 | 1997-11-19 | 波克股份有限公司 | Heat exchanger |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102538397A (en) * | 2012-01-18 | 2012-07-04 | 开封黄河空分集团有限公司 | Process for making nitrogen by air separation or making nitrogen and simultaneously producing oxygen in attached manner |
| CN106403498A (en) * | 2016-09-06 | 2017-02-15 | 广西南宁市邕检科技有限公司 | Novel rotation evaporator |
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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: West Development Zone, Henan province 475000 City Road No. 4 song Applicant before: Kaifeng Huanghe Air Separation Group Co., Ltd. |
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Application publication date: 20111012 |