CN101929790A - High-purity nitrogen equipment - Google Patents
High-purity nitrogen equipment Download PDFInfo
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- CN101929790A CN101929790A CN2010102571663A CN201010257166A CN101929790A CN 101929790 A CN101929790 A CN 101929790A CN 2010102571663 A CN2010102571663 A CN 2010102571663A CN 201010257166 A CN201010257166 A CN 201010257166A CN 101929790 A CN101929790 A CN 101929790A
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- heat exchanger
- main heat
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- oxygen
- purity 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
- F25J3/044—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
- 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
- F25J3/04284—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
- F25J3/04248—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.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/04—Multiple expansion turbines in parallel
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
Abstract
The invention provides high-purity nitrogen equipment which comprises a preprocessing system, a purifying system and a fractionating tower, wherein the fractionating tower comprises a turboexpander, a main heat exchanger and a subcooler for heat exchange, a rectifying tower and a condensation evaporator, the rectifying tower comprises an upper tower and a lower tower, the outlet of the purifying system is connected with the air inlet of the lower tower through a pipeline, and the pipeline passes through the main heat exchanger; the lower tower is also provided with an oxygen-enriched liquid air outlet for oxygen-enriched liquid air generated by rectification to flow out, the oxygen-enriched liquid air outlet is connected with the purifying system through a pipeline, and the pipeline passes through the main heat exchanger; and the upper tower is provided with a nitrogen gas outlet, and the pipeline connected with the outlet passes through the main heat exchanger. In the invention, the pipeline of enriched oxygen, the pipeline of raw material air and the pipeline of nitrogen gas are simultaneously connected with the main heat exchanger, so that the cold quantities of the enriched oxygen and the nitrogen gas are fully utilized, and the high-purity nitrogen equipment saves the energy and protects the environment; meanwhile, the enriched oxygen is sent into the expander for refrigeration, and the high-purity nitrogen equipment has the advantages of reasonable structure, material saving and simple flow configuration.
Description
Technical field
The present invention relates to a kind of high-purity nitrogen plant, relate in particular to the equipment that a kind of method that adopts cryogenic rectification is produced high purity nitrogen.
Background technology
Nitrogen is a kind of application wide industrial gas.It is mainly used in Electronic Packaging/chemical process/illumination/heat treatment/food encapsulation/food product refrigeration/metal manufacturing/glass production/petroleum refining/occasions such as rubber pulverizing/bio-pharmaceuticals.
Present high-purity nitrogen plant mainly adopts the method for cryogenic rectification to produce high purity nitrogen.Rectifying is as the existing history that goes up a century of a kind of traditional separation purification means, and it is widely used in industry-by-industry fields such as metallurgy, chemical industry, glass, electronics.The raw material of high-purity nitrogen plant is an air, and production method mainly is a cryogenic rectification, and main consumption is electric energy in the production process.
World today's science and technology and rapid economic development, all trades and professions increase the demand of nitrogen is anxious, and consumption is increasing, impels air separation plant to make bigger and bigger, and technological process is more and more.The application of high-purity nitrogen plant is also more and more wider, and product nitrogen pressure, purity requirement are had nothing in common with each other.And the high-purity nitrogen plant of band liquid air subcooler only adopts the back oxygen rich air that expands to come the supercooled liquid sky usually, and energy consumption is bigger.
Summary of the invention
The purpose of this invention is to provide a kind of energy-conserving and environment-protective, the high-purity nitrogen plant that energy consumption is low.
Purpose of the present invention realizes by following technical scheme is provided:
A kind of high-purity nitrogen plant, comprise: by the interconnected pretreatment system of pipeline, purification system and fractionating column, described fractionating column comprises turbo-expander, the main heat exchanger and the subcooler that are used for heat exchange, and rectifying column and condenser/evaporator, described rectifying column comprises Shang Ta and Xia Ta, the outlet of described purification system is connected to down the air intake of tower by the road, and this pipeline is through main heat exchanger; Described tower down also is provided with the oxygen-enriched liquid air outlet that is used for for the oxygen-enriched liquid air outflow of rectifying generation, and described oxygen-enriched liquid air outlet is connected to described purification system by the road, and this pipeline is through main heat exchanger; The described tower of going up is provided with nitrogen outlet, and the pipeline that this outlet connects is through main heat exchanger.
Further, described pretreatment system comprises filter, air compressor and the cooling driers that connects successively.
Further, described cooling driers disposes three grades of oil removal filters.
Further, described purification system comprises molecular sieve adsorber and electric heater.
Further, described molecular sieve heater is vertical individual layer bed structure.
Further, described main heat exchanger comprises main heat exchanger top and main heat exchanger bottom.
Further, the pipeline that described oxygen-enriched liquid air outlet connects passes through subcooler, condenser/evaporator, subcooler, main heat exchanger bottom, turbo-expander, subcooler, main heat exchanger bottom, main heat exchanger top successively, is connected to purification system at last.
Further, the pipeline of described oxygen-enriched liquid air outlet connection is connected to the electric heater of purification system.
The present invention makes the cold of oxygen enrichment and nitrogen be fully used energy-conserving and environment-protective by the pipeline of oxygen enrichment, the pipeline of raw air, the pipeline of nitrogen are connected to main heat exchanger simultaneously; Simultaneously oxygen enrichment is sent into decompressor and freeze, rational in infrastructure, saving material, the flow process configuration is simple.High-purity nitrogen plant of the present invention has high reliability, low energy consumption.Nitrogen recovery rate 〉=51%; System of unit nitrogen energy consumption≤0.35kW.h/Nm3N2.
Description of drawings
The invention will be further described below in conjunction with accompanying drawing:
Fig. 1 is the structural representation of specific embodiments of the invention.
1 air cleaner, 15 fractionating columns
3 air compressors, 17 turbo-expanders
5 cooling driers, 19 main heat exchanger tops
7 purification systems, 21 main heat exchanger bottoms
9 molecular sieve adsorbers, 23 subcoolers
11 electric heaters, 25 rectifying columns
13 mufflers, 27 condenser/evaporators
The specific embodiment
Principle of the present invention is to utilize the difference of oxygen nitrogen boiling point in the air, adopts the method for cryogenic rectification to produce high-purity nitrogen.
Following with reference to the description of drawings specific embodiments of the invention.
As Fig. 1, high-purity nitrogen plant of the present invention mainly comprises by the interconnective pretreatment system of pipeline, purification system 7 and fractionating column 15.
Described pretreatment system comprises by the interconnected filter 1 of pipeline, air compressor 3 and cooling driers 5.Described cooling driers 5 has disposed three grades of oil removal filters efficiently, guarantees that its air outlet slit oil content less than 0.003PPm, has reduced the load of purification system 7, has guaranteed the safe and highly efficient operation of purification system 7.The application of cooling driers 5 also makes the air dew points at normal pressure that enters purification system less than-20 ℃, has reduced the consumption of purification system sorbent molecule sieve, has reduced the energy consumption of adsorbent reactivation when reducing cooling driers 5 power consumptions, helps energy-conservation.
Described purification system 7 mainly comprises two molecular sieve adsorbers 9 and electric heater 11.Because the employing of cooling driers 5, make air dew points at normal pressure≤-20 ℃ of molecular sieve adsorber 9 into, the adsorbent consumption that molecular sieve adsorber 9 adsorption moistures need can adopt vertical individual layer bed structure form very little.Molecular sieve adsorber 9 uses remaining moisture content in the part molecular sieve adsorption air, and most of molecular sieve is given full play to the effect of its CO absorption 2 and CnHm, and purifier can be removed to 1PPm with the content of CO2 in the air and H2O.Molecular sieve adsorber adopts the close and equalizing valve door that possess the well-tuned performance of positive and negative stream negotiability, and operating mode is relatively stable in the assurance device regenerative process.Two molecular sieve adsorbers 9 are all with sequential procedure control, and wherein equalizing valve adopts segmentation control, reduce the last tower fluctuation that the molecular sieve pressure equalizing causes.Dirty nitrogen atmospheric valve adopts pre-opened control, reduces the last tower fluctuation that molecular sieve system is switched the rectifying column 25 that causes.The electric heating tube form has structures such as U type pipe, bar-shaped, tube bank.
Described fractionating column 15 mainly comprises two turbo-expanders parallel with one another 17, the main heat exchanger that is used for heat exchange and the subcooler 26 that is interconnected by pipeline, rectifying column 25, condenser/evaporator 27.Wherein main heat exchanger comprises main heat exchanger top 19 and main heat exchanger bottom 21.Rectifying column 25 comprises Shang Ta and Xia Ta.Following tower adopts efficient sieve-plate tower, has promoted the nitrogen recovery rate, and the raising of recovery rate makes that producing the needed air capacity of identical output same purity nitrogen reduces, thereby has greatly reduced energy consumption.Condenser/evaporator 27 adopts the dry type master cold, safer.
The preparation flow of high purity nitrogen below is described in detail in detail.It mainly comprises: the raw air compression---air precooling drying---purification of air---cooling of air---cryogenic rectification---waste expansion refrigeration and product re-heat output.
Raw air filters out impurity such as dust through air cleaner 1, enter then and enter cooling driers 5 after air compressor 3 is compressed to certain pressure, after 5 pairs of input airs of cooling driers carry out cool drying, it is outputed to purification system 7.
Air enters into two molecular sieve adsorbers 9 of purification system 7, disposes airborne water, carbon dioxide, acetylene and other hydrocarbons.Output to fractionating column 15 through the raw air that further purifies.
Raw air at first enters main heat exchanger by the raw air pipeline, and main heat exchanger also is equipped with oxygen enrichment pipeline and nitrogen pipeline.By the raw air pipeline, raw air passes through main heat exchanger top 19 and main heat exchanger bottom 21 successively, carry out heat exchange with the oxygen enrichment and the purity nitrogen of the main heat exchanger of flowing through through oxygen enrichment pipeline and nitrogen pipeline, entered rectifying column 25 from the air intake of the Xia Ta bottom of rectifying column 25 by its cooling back.In rectifying column 25, raw air is separated into down the oxygen-enriched liquid air of tower bottom and the high pure nitrogen of last top of tower.Directly from the top nitrogen opening output of last tower, the process nitrogen pipeline enters main heat exchanger and raw air carries out heat exchange as product nitrogen gas for the part of high pure nitrogen, and with its cooling, itself is exported as product nitrogen gas after the re-heat.Another part of high pure nitrogen outputs to condenser/evaporator 27 by the road from the open top of last tower, the oxygen-enriched liquid air condensation of condenser/evaporator 27 of being flowed through becomes liquid nitrogen, be back to the last tower of rectifying column 25 by the road as the phegma of rectifying column 25, enter Shang Ta by the inlet of the liquid nitrogen on the last tower.
The oxygen-enriched liquid air of following tower bottom is from the oxygen-enriched liquid air outlet output of Xia Ta bottom, after the oxygen enrichment pipeline is flowed through subcooler 23, enter condenser/evaporator 27 and carry out heat exchange, the subcooler 23 of flowing through once more after the intensification, go out subcooler 23 backs and flow into main heat exchanger bottom 21 recovery section colds, enter turbo-expander 17 then, in turbo-expander 17, carry out swell refrigeration, oxygen-enriched stream after the expansion is from turbo-expander 17 outputs, enter in the subcooler 23 to cross and enter main heat exchanger once more after cold and carry out heat exchange with oxygen-enriched liquid air, raw air is cooled off, flow into the electric heater 11 of purification system 7 then, import molecular sieve adsorber 9 as regeneration gas, oxygen rich air unnecessary in the turbo-expander 17 is released in the air through a muffler 13 thereupon.
The oxygen-enriched liquid air that obtains of rectifying column 25 and the cold of nitrogen all are used to cool off raw air by main heat exchanger, the capacity usage ratio height in the present embodiment.
What need understand is: above-mentioned explanation is not to be limitation of the present invention, and in the present invention conceived scope, the interpolation of being carried out, conversion, replacement etc. also should belong to protection scope of the present invention.
Claims (8)
1. high-purity nitrogen plant, comprise: by the interconnected pretreatment system of pipeline, purification system and fractionating column, described fractionating column comprises turbo-expander, the main heat exchanger and the subcooler that are used for heat exchange, and rectifying column and condenser/evaporator, described rectifying column comprises Shang Ta and Xia Ta, it is characterized in that: the outlet of described purification system is connected to down the air intake of tower by the road, and this pipeline is through main heat exchanger; Described tower down also is provided with the oxygen-enriched liquid air outlet that is used for for the oxygen-enriched liquid air outflow of rectifying generation, and described oxygen-enriched liquid air outlet is connected to described purification system by the road, and this pipeline is through main heat exchanger; The described tower of going up is provided with nitrogen outlet, and the pipeline that this outlet connects is through main heat exchanger.
2. high-purity nitrogen plant according to claim 1 is characterized in that, described pretreatment system comprises filter, air compressor and the cooling driers that connects successively.
3. high-purity nitrogen plant according to claim 2 is characterized in that, described cooling driers disposes three grades of oil removal filters.
4. high-purity nitrogen plant according to claim 1 is characterized in that described purification system comprises molecular sieve adsorber and electric heater.
5. high-purity nitrogen plant according to claim 4 is characterized in that, described molecular sieve heater is vertical individual layer bed structure.
6. high-purity nitrogen plant according to claim 1 is characterized in that, described main heat exchanger comprises main heat exchanger top and main heat exchanger bottom.
7. high-purity nitrogen plant according to claim 6, it is characterized in that, the pipeline that described oxygen-enriched liquid air outlet connects passes through subcooler, condenser/evaporator, subcooler, main heat exchanger bottom, turbo-expander, subcooler, main heat exchanger bottom, main heat exchanger top successively, is connected to purification system at last.
8. high-purity nitrogen plant according to claim 7 is characterized in that, the pipeline that described oxygen-enriched liquid air outlet connects is connected to the electric heater of purification system.
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| CN2010102571663A CN101929790B (en) | 2010-08-19 | 2010-08-19 | High-purity nitrogen equipment |
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| CN2010102571663A CN101929790B (en) | 2010-08-19 | 2010-08-19 | High-purity nitrogen equipment |
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| CN101929790B CN101929790B (en) | 2012-07-18 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102322726A (en) * | 2011-06-13 | 2012-01-18 | 开封空分集团有限公司 | Air separating device and method for alternatively producing nitrogen gas and liquid nitrogen |
| CN102320581A (en) * | 2011-08-30 | 2012-01-18 | 开封黄河空分集团有限公司 | A kind of nitrogen reparation technology |
| CN102494515A (en) * | 2011-12-05 | 2012-06-13 | 无锡威克亨盛机械制造有限公司 | Process for preparing high-pressure medical oxygen |
| 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 |
| CN104034123A (en) * | 2014-06-27 | 2014-09-10 | 莱芜钢铁集团有限公司 | Liquid loading and purity regulating integration operation method of air separation plant |
| CN104807290A (en) * | 2015-04-29 | 2015-07-29 | 河南开元空分集团有限公司 | Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion |
| CN105823074A (en) * | 2016-05-06 | 2016-08-03 | 碧海舟（北京）节能环保装备有限公司 | Oxygen-enriched and energy-saving combustion system capable of achieving zero emission of nitrogen oxides |
| CN107345737A (en) * | 2017-06-08 | 2017-11-14 | 苏州制氧机股份有限公司 | The double condensation stream backed expansion nitrogen making machines of double tower and its method for preparing nitrogen |
| CN114413570A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5964104A (en) * | 1997-05-15 | 1999-10-12 | Linde Aktiengesellschaft | Method and device for obtaining nitrogen by low-temperature separation of air |
| JP2005188796A (en) * | 2003-12-25 | 2005-07-14 | Taiyo Nippon Sanso Corp | Nitrogen producing method and device |
| CN1645022A (en) * | 2005-03-07 | 2005-07-27 | 杭州凯德空分设备有限公司 | Air separated rectifying process and air separating apparatus |
| JP2007147113A (en) * | 2005-11-24 | 2007-06-14 | Taiyo Nippon Sanso Corp | Nitrogen manufacturing method and device |
| CN101033909A (en) * | 2007-04-11 | 2007-09-12 | 杭州杭氧股份有限公司 | Air separation system for generating liquid oxygen and liquid nitrogen |
| CN201265997Y (en) * | 2008-09-05 | 2009-07-01 | 苏州制氧机有限责任公司 | Liquid air separation plant |
| CN101492156A (en) * | 2009-03-12 | 2009-07-29 | 四川空分设备(集团)有限责任公司 | Low-energy consumption nitrogen production method and apparatus |
| CN201281522Y (en) * | 2008-08-22 | 2009-07-29 | 苏州制氧机有限责任公司 | Oxygen self-supercharging air separating device |
| CN201377961Y (en) * | 2008-09-09 | 2010-01-06 | 苏州制氧机有限责任公司 | Multi-operating mode air separation equipment |
| CN201753264U (en) * | 2010-08-19 | 2011-03-02 | 苏州制氧机有限责任公司 | High-purity nitrogen device |
-
2010
- 2010-08-19 CN CN2010102571663A patent/CN101929790B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5964104A (en) * | 1997-05-15 | 1999-10-12 | Linde Aktiengesellschaft | Method and device for obtaining nitrogen by low-temperature separation of air |
| JP2005188796A (en) * | 2003-12-25 | 2005-07-14 | Taiyo Nippon Sanso Corp | Nitrogen producing method and device |
| CN1645022A (en) * | 2005-03-07 | 2005-07-27 | 杭州凯德空分设备有限公司 | Air separated rectifying process and air separating apparatus |
| JP2007147113A (en) * | 2005-11-24 | 2007-06-14 | Taiyo Nippon Sanso Corp | Nitrogen manufacturing method and device |
| CN101033909A (en) * | 2007-04-11 | 2007-09-12 | 杭州杭氧股份有限公司 | Air separation system for generating liquid oxygen and liquid nitrogen |
| CN201281522Y (en) * | 2008-08-22 | 2009-07-29 | 苏州制氧机有限责任公司 | Oxygen self-supercharging air separating device |
| CN201265997Y (en) * | 2008-09-05 | 2009-07-01 | 苏州制氧机有限责任公司 | Liquid air separation plant |
| CN201377961Y (en) * | 2008-09-09 | 2010-01-06 | 苏州制氧机有限责任公司 | Multi-operating mode air separation equipment |
| CN101492156A (en) * | 2009-03-12 | 2009-07-29 | 四川空分设备(集团)有限责任公司 | Low-energy consumption nitrogen production method and apparatus |
| CN201753264U (en) * | 2010-08-19 | 2011-03-02 | 苏州制氧机有限责任公司 | High-purity nitrogen device |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102322726A (en) * | 2011-06-13 | 2012-01-18 | 开封空分集团有限公司 | Air separating device and method for alternatively producing nitrogen gas and liquid nitrogen |
| CN102320581A (en) * | 2011-08-30 | 2012-01-18 | 开封黄河空分集团有限公司 | A kind of nitrogen reparation technology |
| CN102494515A (en) * | 2011-12-05 | 2012-06-13 | 无锡威克亨盛机械制造有限公司 | Process for preparing high-pressure medical oxygen |
| 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 |
| 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 |
| CN104034123A (en) * | 2014-06-27 | 2014-09-10 | 莱芜钢铁集团有限公司 | Liquid loading and purity regulating integration operation method of air separation plant |
| CN104807290A (en) * | 2015-04-29 | 2015-07-29 | 河南开元空分集团有限公司 | Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion |
| CN105823074A (en) * | 2016-05-06 | 2016-08-03 | 碧海舟（北京）节能环保装备有限公司 | Oxygen-enriched and energy-saving combustion system capable of achieving zero emission of nitrogen oxides |
| CN107345737A (en) * | 2017-06-08 | 2017-11-14 | 苏州制氧机股份有限公司 | The double condensation stream backed expansion nitrogen making machines of double tower and its method for preparing nitrogen |
| CN107345737B (en) * | 2017-06-08 | 2023-09-19 | 苏州制氧机股份有限公司 | Double-tower double-condensation reflux expansion nitrogen making machine and nitrogen making method thereof |
| CN114413570A (en) * | 2022-01-19 | 2022-04-29 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
| CN114413570B (en) * | 2022-01-19 | 2023-01-31 | 四川空分设备(集团)有限责任公司 | Double-tower floor type nitrogen making device |
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Address after: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee after: SUZHOU OXYGEN PLANT CO., LTD. Address before: Wuzhong District Mudu town Suzhou city Jiangsu province 215101 Spring Road No. 31 Patentee before: Suzhou Oxygen Plant Co., Ltd. |