CN101929790B - High-purity nitrogen equipment - Google Patents

High-purity nitrogen equipment Download PDF

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Publication number
CN101929790B
CN101929790B CN2010102571663A CN201010257166A CN101929790B CN 101929790 B CN101929790 B CN 101929790B CN 2010102571663 A CN2010102571663 A CN 2010102571663A CN 201010257166 A CN201010257166 A CN 201010257166A CN 101929790 B CN101929790 B CN 101929790B
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CN
China
Prior art keywords
heat exchanger
main heat
pipeline
oxygen
tower
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CN2010102571663A
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Chinese (zh)
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CN101929790A (en
Inventor
胡玖益
张小元
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苏州制氧机有限责任公司
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Priority to CN2010102571663A priority Critical patent/CN101929790B/en
Publication of CN101929790A publication Critical patent/CN101929790A/en
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Publication of CN101929790B publication Critical patent/CN101929790B/en

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Classifications

    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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

High-purity nitrogen plant

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/made/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 supercooled liquid empty 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.

The object of the invention is realized through following technical scheme is provided:

A kind of high-purity nitrogen plant comprises: through the interconnected pretreatment system of pipeline, purification system and fractionating column; Said fractionating column comprises turbo-expander; The main heat exchanger and the subcooler that are used for heat exchange, and rectifying column and condenser/evaporator, said rectifying column comprises Shang Ta and Xia Ta; The outlet of said purification system is connected to down the air intake of tower by the road, and this pipeline is through main heat exchanger; Said down tower also is provided with the oxygen-enriched liquid air outlet that the oxygen-enriched liquid air that is used to supply rectifying to produce flows out, and said oxygen-enriched liquid air outlet is connected to said purification system by the road, and this pipeline is through main heat exchanger; The said tower of going up is provided with nitrogen outlet, and the pipeline that this outlet connects is through main heat exchanger.

Further, said pretreatment system comprises filter, air compressor and the cooling driers that connects successively.

Further, said cooling driers disposes three grades of oil removal filters.

Further, said purification system comprises molecular sieve adsorber and electric heater.

Further, said molecular sieve heater is vertical individual layer bed structure.

Further, said main heat exchanger comprises main heat exchanger top and main heat exchanger bottom.

Further, the pipeline that said 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 said 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 through 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

Below in conjunction with accompanying drawing the present invention is described further:

Fig. 1 is the structural representation of specific embodiment of the present 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 description of drawings specific embodiment of the present invention.

Like Fig. 1, high-purity nitrogen plant of the present invention mainly comprises through the interconnective pretreatment system of pipeline, purification system 7 and fractionating column 15.

Described pretreatment system comprises through the interconnected filter of pipeline 1, 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 gets into purification system less than-20 ℃, has reduced the consumption of purification system sorbent molecule sieve, when reducing cooling driers 5 power consumptions, has reduced the energy consumption of adsorbent reactivation, 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 through 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 detailed.It mainly comprises: the raw air compression---air precooling is dry---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, get into then to get into 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.Raw air through further purifying outputs to fractionating column 15.

Raw air at first gets into main heat exchanger through the raw air pipeline, and main heat exchanger also is equipped with oxygen enrichment pipeline and nitrogen pipeline.Through 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 oxygen enrichment and the purity nitrogen of the main heat exchanger of flowing through through oxygen enrichment pipeline and nitrogen pipeline, by its cooling afterwards from the air intake entering rectifying column 25 of the Xia Ta bottom of rectifying column 25.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.The part of high pure nitrogen directly from the top nitrogen opening output of last tower, is carried out heat exchange through nitrogen pipeline entering main heat exchanger and raw air as product nitrogen gas, 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, get into by the inlet of the liquid nitrogen on the last tower and go up 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, get into condenser/evaporator 27 and carry out heat exchange, the subcooler 23 of flowing through once more after the intensification goes out subcooler 23 backs and flows into main heat exchanger bottom 21 recovery section colds; Get into turbo-expander 17 then; In turbo-expander 17, carry out swell refrigeration, the oxygen-enriched stream after the expansion is from turbo-expander 17 output, gets in the subcooler 23 to cross with oxygen-enriched liquid air to get into main heat exchanger once more after cold and carry out heat exchange; Raw air is cooled off; Flow into the electric heater 11 of purification system 7 then, import molecular sieve adsorber 9 as regeneration gas thereupon, oxygen rich air unnecessary in the turbo-expander 17 is released in the air through a muffler 13.

The oxygen-enriched liquid air that rectifying column 25 obtains in this embodiment and the cold of nitrogen all are used to cool off raw air through main heat exchanger, and capacity usage ratio is high.

What need understand is: above-mentioned explanation is not to be limitation of the present invention, and in concept of the present invention, the interpolation of being carried out, conversion, replacement etc. also should belong to protection scope of the present invention.

Claims (8)

1. a high-purity nitrogen plant comprises: through the interconnected pretreatment system of pipeline, purification system and fractionating column; Said fractionating column comprises turbo-expander; The main heat exchanger and the subcooler that are used for heat exchange, and rectifying column and condenser/evaporator, said rectifying column comprises Shang Ta and Xia Ta; It is characterized in that: the outlet of said purification system is connected to down the air intake of tower by the road, and this pipeline is through main heat exchanger; Said down tower also is provided with the oxygen-enriched liquid air outlet that the oxygen-enriched liquid air that is used to supply rectifying to produce flows out, and said oxygen-enriched liquid air outlet is connected to said purification system by the road, and this pipeline is through main heat exchanger; The said 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, said 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, said cooling driers disposes three grades of oil removal filters.
4. high-purity nitrogen plant according to claim 1 is characterized in that said purification system comprises molecular sieve adsorber and electric heater.
5. high-purity nitrogen plant according to claim 4 is characterized in that, said molecular sieve adsorber is vertical individual layer bed structure.
6. high-purity nitrogen plant according to claim 1 is characterized in that, said 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 said 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 said oxygen-enriched liquid air outlet connects is connected to the electric heater of purification system.
CN2010102571663A 2010-08-19 2010-08-19 High-purity nitrogen equipment CN101929790B (en)

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CN101929790B true CN101929790B (en) 2012-07-18

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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
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
CN104034123B (en) * 2014-06-27 2016-05-18 莱芜钢铁集团有限公司 A kind of air-separating plant hydrops is adjusted pure integration operation method
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

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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.

C56 Change in the name or address of the patentee