CN1436995A - Method of recovering oxygen, nitrogen and air exhausted from air separator - Google Patents
Method of recovering oxygen, nitrogen and air exhausted from air separator Download PDFInfo
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- CN1436995A CN1436995A CN 02100593 CN02100593A CN1436995A CN 1436995 A CN1436995 A CN 1436995A CN 02100593 CN02100593 CN 02100593 CN 02100593 A CN02100593 A CN 02100593A CN 1436995 A CN1436995 A CN 1436995A
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
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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
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
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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
- F25J3/04309—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 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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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
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The present invention is method of recovering oxygen and nitrogen during air separation. One system is constituted with the spare expander of air separator, one increased heat exchanger, some pipes and valves. Air pumped by the main heat exchanger in the air separator, exhausted and pressureized air after compression, purification and cooling or exhausted and pressurized nitrogen after cooling in the heat exchanger is expanded in the space expander and used as cooling work medium, and liquefied in the heat exchanger into liquid oxygen or liquid nitrogen, and the liquid oxygen or liquid nitrogen is collected in the liquid oxygen or liquid nitrogen storage. Meanwhile, the temperature of the exhausted air from the expander may be controlled to liquefy partially the exhausted air or nitrogen.
Description
Technical field
Reclaim oxygen, the nitrogen of emptying, the method for air when the present invention relates to air separation, relate in particular to air separation oxygen, nitrogen, air liquefaction recovery method to emptying when preparing oxygen and/or nitrogen.
Background technology
Existing air separation (method by low-temperature liquefaction and rectifying is separated) technology is generally: the compressed purifying (dedusting of air, compression, air cooling removes moisture and molecular sieve adsorption is removed moisture and carbon dioxide) laggardly go into main heat exchanger, after the main heat exchanger cooling, enter rectifying column, in rectifying column, carry out air separation, isolate nitrogen and/or oxygen, after the main heat exchanger heat exchange, obtain normal pressure nitrogen and/or oxygen from rectifying column separated nitrogen and/or oxygen, after the nitrogen of main heat exchanger and/or the general compressed machine pressurization of oxygen, send into process units by pipeline, wherein said main heat exchanger, decompressor, rectifying columns etc. are placed in the ice chest.On the one hand, when rectifying column carries out air separation, need to descend the oxygen-enriched air of tower and the part air of main heat exchanger middle part extraction to send into tower participation rectifying by decompressor together, in order to guarantee the continuous running of air separation unit, generally need standby one or two decompressors, when normal operation, has only a decompressor in work.On the other hand, in the general air separation unit designed capacity of compressor a little more than the disposal ability of rectifier unit, like this will some air enter that molecular sieve adsorber dewaters and carbon dioxide before emptying; And nitrogen that obtains through air separation and/or oxygen are also often greater than the demand of process units, also can some nitrogen and/or oxygen or going out main heat exchanger and emptying after compression or recovery, prior art generally adopts the recovery of emptying oxygen and/or nitrogen increases the new gas liquefaction device of a cover, invests bigger.
Summary of the invention
The purpose of this invention is to provide in a kind of air separation unit the method for the oxygen that reclaims emptying, nitrogen, air, this method has been utilized the standby decompressor of air separation unit, invests lessly, has improved the utilization rate of air separation unit existing equipment simultaneously.
Technical scheme of the present invention is to utilize the standby decompressor of air separation unit, increase a heat exchanger (as liquefier) again, use some pipelines again, valves etc. are with aforesaid decompressor, heat exchangers etc. are formed a system, be used to air (bleeding in the abbreviation) from the main heat exchanger middle part extraction of air separation unit, the emptying air with pressure that obtains after the compressed purification cooling or press nitrogen after the standby decompressor of air separation unit expands, to do refrigeration working medium through the emptying band of heat exchanger cooling, in heat exchanger, press nitrogen or emptying band to press oxygen liquid to change into liquid nitrogen or liquid oxygen on the emptying band, thereby reach the oxygen that from air separation unit, reclaims emptying, nitrogen, the purpose of air.
As previously mentioned: the designed capacity of compressor is a little more than the disposal ability of rectifier unit in the general air separation unit, like this will some air enter that molecular sieve adsorber dewaters and carbon dioxide before emptying, the air of this part emptying can be used as refrigeration working medium of the present invention, on the other hand, when the air capacity that is used as refrigeration working medium is not enough, and the amount of nitrogen that obtains through air separation and/or oxygen is during greater than the demand of process units, also can adopt the change working condition, reduce the amount of device output oxygen and/or nitrogen, so also can save air, this part air also can be used as refrigeration working medium.When doing refrigeration working medium with air, can air be extracted out from the diverse location of air separation unit and do refrigeration working medium: a kind of method is that the compressed back air with pressure (being the emptying air with pressure) more than needed that purifies is done refrigeration working medium; Another kind method is to make air with pressure after the compressed purification enter into the main heat exchanger of air separation unit, and then from main heat exchanger, extract air (bleeding promptly) more than needed out as refrigeration working medium, the main heat exchanger warm end temperature difference of air separation unit is dwindled, reduce cold damage, voluminous liquid.In addition, also can do refrigeration working medium with separated nitrogen.When being refrigeration working medium, can press nitrogen directly to send into process units on the band that the user needs, and the band that will surpass user's requirement press nitrogen (being emptying band pressure nitrogen) do refrigeration working medium with after compression through the nitrogen of main heat exchanger with nitrogen.Consider from energy-conservation angle, the present invention preferably with in bleed and the emptying air with pressure as refrigeration working medium.
The present invention reclaims the method for oxygen, nitrogen, air of emptying from air separation unit different slightly variant because of refrigeration working medium, will describe in detail below.
Particularly, when after the decompressor that heat exchanger cools off and air separation unit is standby expands, doing refrigeration working medium with the emptying air with pressure that obtains after the compression purification, its detailed process is: will compress the part emptying air with pressure that obtains after purifying and send in the heat exchanger, obtain cold air stream after cooling by heat exchanger, at least a portion cold air stream and part are not converged the standby decompressor inlet that is sent to air separation unit by the emptying air with pressure of heat exchanger, adjusting makes the temperature of air satisfy temperature (temperature that is air is near its condensing temperature) at the decompressor inlet by the air capacity of heat exchanger and the air capacity by heat exchanger not, and the air of decompressor outlet goes regenerated molecular sieve or emptying behind heat exchanger; After being liquefied, the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive the decompressor outlet air in heat exchanger is sent in liquid nitrogen/liquid oxygen accumulator tanks.When doing refrigeration working fluid with the emptying air with pressure, normal pressure nitrogen becomes band after compression and presses nitrogen, afterwards whole emptying bands is pressed nitrogen to send in the heat exchanger to reclaim liquid nitrogen.
Particularly, press nitrogen after the standby decompressor of air separation unit expands, to do refrigeration working medium with the cooled band of heat exchanger, its detailed process is: with normal pressure nitrogen after nitrogen compressor pressurization, press nitrogen to send in the heat exchanger on a part of emptying band wherein, obtain cold nitrogen stream after cooling by heat exchanger, do not press nitrogen to converge with part the cold nitrogen stream of at least a portion and be sent to the standby decompressor inlet of air separation unit by the emptying band of heat exchanger, adjusting makes nitrogen temperature satisfy temperature (temperature that is nitrogen is near its condensing temperature) at the decompressor inlet by the nitrogen amount of heat exchanger and the nitrogen amount by heat exchanger not, and the nitrogen of decompressor outlet converges the back cycling and reutilization or removes regenerated molecular sieve or emptying with normal pressure nitrogen behind heat exchanger; After being liquefied, the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive decompressor outlet nitrogen in heat exchanger is sent in liquid nitrogen/liquid oxygen accumulator tanks.When doing refrigeration working fluid with nitrogen, normal pressure nitrogen becomes band after compression and presses nitrogen, and band presses nitrogen to be divided into three parts afterwards: a part is as the raw material of system liquid nitrogen; In addition two parts are as refrigeration working medium: promptly converge through the nitrogen of heat exchanger and the nitrogen that do not pass through heat exchanger and send into behind decompressor again and do refrigeration working medium in the heat exchanger.
Particularly, with in bleed when after the standby decompressor of air separation unit expands, doing refrigeration working medium, its detailed process is: will in bleed and be sent to the standby decompressor inlet of air separation unit, the air of decompressor outlet goes regenerated molecular sieve or emptying behind heat exchanger; To be with and press oxygen or band to press nitrogen to send in the heat exchanger, be sent in liquid nitrogen/liquid oxygen accumulator tanks after the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive the decompressor outlet air in heat exchanger is liquefied.With in bleed when doing refrigeration working medium, normal pressure nitrogen becomes band after compression and presses nitrogen, afterwards whole emptying bands is pressed nitrogen to send in the heat exchanger to reclaim liquid nitrogen.
The disclosed various heat exchangers of prior art all can be used for the present invention, as select plate-fin heat exchanger or pipe heat exchanger.From angle consideration energy-conservation and that save the space, the preferred plate-fin heat exchanger of the present invention.Heat exchanger can be arranged in the ice chest of air separation unit and main device accomplishes that cold damage is complementary, and therefore being equivalent to liquefaction system is in the vacuum heat-preserving state, and cold damage greatly reduces, and has further improved liquefaction efficiency.Heat exchanger can be integrated with main heat exchanger, also can be arranged with the main heat exchanger branch, with one independently heat exchanger place in the ice chest.
The standby decompressor of air separation unit all can be used for the present invention, as can be low-pressure expansion machine or booster expansion machine.
A cooling working medium part of the present invention is through the heat exchanger cooling, a part is cooled off without superheater, after converging, this two parts cooling working medium is sent to the standby decompressor inlet of air separation unit, adjusting makes nitrogen temperature satisfy temperature at the decompressor inlet by the nitrogen amount of heat exchanger and the nitrogen amount by heat exchanger not, and the temperature that decompressor is gone into implication is preferably-125～-150 ℃.
The present invention also can make described cold air stream or cold nitrogen stream partial liquefaction by controlling the temperature that decompressor is worked off one's feeling vent one's spleen, and receives liquid air or the liquid nitrogen of collecting gained with liquid nitrogen/liquid air accumulator tanks.
Normal pressure nitrogen of the present invention is from the isolated nitrogen behind main heat exchanger of rectifying column.
It is from the isolated oxygen more than needed behind main heat exchanger and compressor of rectifying column that emptying band of the present invention is pressed oxygen; It is from the isolated nitrogen more than needed behind main heat exchanger and compressor of rectifying column that described emptying band is pressed nitrogen; The emptying air with pressure anhydrates and the more than needed air of molecular sieve adsorption after removing moisture and carbon dioxide for removing through dedusting, compression, air cooling.
Method of the present invention has been utilized the standby decompressor of air separation unit, invest less, also improved the utilization rate of air separation unit existing equipment, make that simultaneously the standby property of decompressor is stronger, more timely, safer, decompressor has been accomplished dynamic cold standby car rather than the static car that is equipped with of normal temperature, and the decompressor switching does not have any disturbance to king-tower.
Method of the present invention can be produced liquid oxygen, liquid nitrogen, liquid air product respectively.Also can accomplish to be interrupted liquefaction, further improve the comprehensive utilization ratio of device.Flow process is simple, and is easy to operate, safe.Air compressor machine is moved under a kind of operating mode for a long time, and operating condition is more away from the surging point.
These and other purposes of the present invention, feature and advantage will become more clear after reading this specification with reference to the following drawings.
Description of drawings
Fig. 1 is for implementing the recovery liquefaction flow path figure of the inventive method
The specific embodiment
The present invention will be further described below in conjunction with accompanying drawing, but do not limit to scope of the present invention.
When being cooling working medium: in Fig. 1 with the emptying air with pressure, the part emptying air with pressure that obtains after the compression purification is sent in the heat exchanger 16 by valve 1, obtain cold air stream after cooling by heat exchanger 16, its temperature is-156 ℃～-168 ℃, with at least a portion cold air stream by valve 10 with partly not the air with pressure (temperature is 10～20 ℃) by heat exchanger by converging the inlet of the standby decompressor 17 that is sent to air separation unit behind the valve 8, the air capacity of adjusting by heat exchanger 16 and valve 8 and air capacity by valve 10 make the temperature of converging the back air satisfy inlet temperature at decompressor 17, preferred-125 ℃～-150 ℃ of decompressor 17 inlet air temperature degree, the decompressor temperature of working off one's feeling vent one's spleen is preferably-162 ℃～-185 ℃, pressure is preferably 0.11-0.15Mpa, the air of decompressor 17 outlets is behind heat exchanger 16, cold is passed to oxygen, nitrogen, air, after expanded air goes out heat exchange liquefier 16, temperature is about 5 ℃～10 ℃, removes regenerated molecular sieve or passes through valve 14 emptying by valve 13 more afterwards; After being liquefied, the cold that band presses nitrogen to press oxygen to receive decompressor 17 outlet airs by valve 5 in heat exchanger 16 by valve 4 or emptying band is sent in liquid nitrogen/liquid oxygen accumulator tanks 18.The present invention also can be by control decompressor 17 temperature of working off one's feeling vent one's spleen, and makes described cold air stream partial liquefaction and is collected in liquid nitrogen/liquid air accumulator tanks 19.In addition, also can by valve 12 cold air in liquid air/liquid nitrogen accumulator tanks 19 is emitted and converge with the air of decompressor 17 outlet after do refrigeration working medium.When air separation unit need be with standby decompressor, can close other liquefaction valves and realize by opening 9 valves 7 and valve 11.
When being cooling working medium with band pressure nitrogen, in Fig. 1, normal pressure nitrogen is divided into three parts after the nitrogen compressor pressurization: a part is sent into process units by valve 2 and is satisfied user's needs, and the part in the band pressure nitrogen stream more than needed (the emptying band is pressed nitrogen) is as cooling working medium; Another part is as the raw material that reclaims liquid nitrogen.Part emptying band presses nitrogen to send in the heat exchanger 16 by valve 3, obtain cold nitrogen stream after cooling by heat exchanger 16, its temperature is-156 ℃～-168 ℃, do not press nitrogen (temperature is 15～25 ℃) by converging the inlet of the standby decompressor 17 that is sent to air separation unit behind the valve 8 by valve 10 and part the cold nitrogen stream of at least a portion by the emptying band of heat exchanger, the temperature of converging back nitrogen that makes the nitrogen amount of adjusting by heat exchanger 16 and valve 8 and nitrogen amount by valve 10 satisfies the inlet temperature at decompressor 17, preferred-125 ℃～-150 ℃ of decompressor 17 inlet air temperature degree, the decompressor temperature of working off one's feeling vent one's spleen is preferably-162 ℃～-185 ℃, pressure is preferably 0.11-0.15Mpa, decompressor 17 outlet nitrogen are behind heat exchanger 16, cold is passed to oxygen or nitrogen, after expansion nitrogen goes out heat exchange liquefier 16, temperature is about 5 ℃～10 ℃, converges the back cycling and reutilization by valve 15 and normal pressure nitrogen more afterwards, remove regenerated molecular sieve or pass through valve 14 emptying by valve 13; After being liquefied, the cold that part emptying band presses nitrogen to press oxygen to receive decompressor 17 outlet airs by valve 5 in heat exchanger 16 by valve 4 or emptying band is sent in liquid nitrogen/liquid oxygen accumulator tanks 18.The present invention also can be by control decompressor 17 temperature of working off one's feeling vent one's spleen, and makes described cold nitrogen stream partial liquefaction and is collected in liquid nitrogen/liquid air accumulator tanks 19.In addition, also can by valve 12 with the cold air in liquid air/liquid nitrogen accumulator tanks 19 or cold nitrogen is emitted and converge with the air of decompressor 17 outlet after do refrigeration working medium.When air separation unit need be with standby decompressor, can be by closing other liquefaction valves and realize by opening 9 valves 7 and valve 11.
With in when bleeding to cooling working medium: in Fig. 1, to send into the inlet of the standby decompressor 17 of air separation unit from the gas (bleeding in the abbreviation) that extract out at the heat exchange liquefier middle part of air separation unit by valve 6, the decompressor temperature of working off one's feeling vent one's spleen is preferably-162 ℃～-185 ℃, pressure is preferably 0.11-0.15Mpa, the air of decompressor 17 outlets is behind heat exchanger 16, cold is passed to oxygen, nitrogen, air, after expanded air goes out heat exchange liquefier 16, temperature is about 5 ℃～10 ℃, removes regenerated molecular sieve or passes through valve 14 emptying by valve 13 more afterwards; After being liquefied, the cold that the emptying band presses nitrogen to press oxygen to receive decompressor 17 outlet airs by valve 5 in heat exchanger 16 by valve 4 or emptying band is sent in liquid nitrogen/liquid oxygen accumulator tanks 18.The present invention also can be by control decompressor 17 temperature of working off one's feeling vent one's spleen, and makes described cold air stream partial liquefaction and is collected in liquid nitrogen/liquid air accumulator tanks 19.When air separation unit need be with standby decompressor, can close other liquefaction valves and realize by opening 9 valves 7 and valve 11 by opening.
Claims (12)
1, the method for the oxygen of recovery emptying, nitrogen, air in a kind of air separation unit, it is characterized in that and to press nitrogen after the standby decompressor expansion of air separation unit, to do refrigeration working medium from the emptying air with pressure that obtains after the air of extracting out in the middle part of the main heat exchanger of air separation unit (bleeding in the abbreviation), the compressed purification cooling or through the emptying band of heat exchanger cooling, in heat exchanger, press nitrogen or emptying band to press oxygen liquid to change into liquid nitrogen or liquid oxygen on the emptying band.
2, the described method of claim 1, it is characterized in that after the decompressor that heat exchanger cools off and air separation unit is standby expands, doing refrigeration working medium with the emptying air with pressure that obtains after the compression purification, its detailed process is: will compress the part emptying air with pressure that obtains after purifying and send in the heat exchanger, obtain cold air stream after cooling by heat exchanger, at least a portion cold air stream and part are not converged the standby decompressor inlet that is sent to air separation unit by the emptying air with pressure of heat exchanger, adjusting makes the temperature of air satisfy temperature at the decompressor inlet by the air capacity of heat exchanger and the air capacity by heat exchanger not, and the air of decompressor outlet goes regenerated molecular sieve or emptying behind heat exchanger; After being liquefied, the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive the decompressor outlet air in heat exchanger is sent in liquid nitrogen/liquid oxygen accumulator tanks.
3, the described method of claim 1, it is characterized in that pressing nitrogen after the standby decompressor of air separation unit expands, to do refrigeration working medium with the cooled band of heat exchanger, its detailed process is: with normal pressure nitrogen after nitrogen compressor pressurization, press nitrogen to send in the heat exchanger on a part of emptying band wherein, obtain cold nitrogen stream after cooling by heat exchanger, do not press nitrogen to converge with part the cold nitrogen stream of at least a portion and be sent to the standby decompressor inlet of air separation unit by the emptying band of heat exchanger, adjusting makes nitrogen temperature satisfy temperature at the decompressor inlet by the nitrogen amount of heat exchanger and the nitrogen amount by heat exchanger not, and the nitrogen of decompressor outlet converges the back cycling and reutilization or removes regenerated molecular sieve or emptying with normal pressure nitrogen behind heat exchanger; After being liquefied, the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive decompressor outlet nitrogen in heat exchanger is sent in liquid nitrogen/liquid oxygen accumulator tanks.
4, the described method of claim 1, it is characterized in that with in bleed and after the standby decompressor of air separation unit expands, do refrigeration working medium, its detailed process is: bleeding in inciting somebody to action is sent to the standby decompressor inlet of air separation unit, and the air of decompressor outlet goes regenerated molecular sieve or emptying behind heat exchanger; To be with and press oxygen or band to press nitrogen to send in the heat exchanger, be sent in liquid nitrogen/liquid oxygen accumulator tanks after the cold that the emptying band presses nitrogen or emptying band to press oxygen to receive the decompressor outlet air in heat exchanger is liquefied.
5, each described method of claim 1-4 is characterized in that described heat exchanger is a plate-fin heat exchanger.
6, each described method of claim 1-5 is characterized in that described heat exchanger is arranged in the ice chest of air separation unit.
7, each described method of claim 1-6 is characterized in that described decompressor is standby low-pressure expansion machine of air separation unit or booster expansion machine.
8, each described method of claim 1-7 is characterized in that it is-125～-150 ℃ that decompressor is gone into the temperature of implication.
9, claim 1,2 or 4 described methods is characterized in that the part of described cold air flow liquidization is sent in liquid nitrogen/liquid air accumulator tanks.
10, the described method of claim 3 is characterized in that the part of described cold nitrogen flow liquidization is sent in liquid nitrogen/liquid air accumulator tanks.
11, the described method of claim 3 is characterized in that described normal pressure nitrogen is from the isolated nitrogen behind main heat exchanger of rectifying column
12, each described method of claim 1-11 is characterized in that it is from the isolated oxygen more than needed behind main heat exchanger and compressor of rectifying column that described emptying band is pressed oxygen; It is from the isolated nitrogen more than needed behind main heat exchanger and compressor of rectifying column that described emptying band is pressed nitrogen; The emptying air with pressure anhydrates and the more than needed air of molecular sieve adsorption after removing moisture and carbon dioxide for removing through dedusting, compression, air cooling.
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| CN 02100593 CN1239875C (en) | 2002-02-07 | 2002-02-07 | Method of recovering oxygen, nitrogen and air exhausted from air separator |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02100593 CN1239875C (en) | 2002-02-07 | 2002-02-07 | Method of recovering oxygen, nitrogen and air exhausted from air separator |
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| CN1436995A true CN1436995A (en) | 2003-08-20 |
| CN1239875C CN1239875C (en) | 2006-02-01 |
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| CN 02100593 Expired - Fee Related CN1239875C (en) | 2002-02-07 | 2002-02-07 | Method of recovering oxygen, nitrogen and air exhausted from air separator |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102155626A (en) * | 2010-12-30 | 2011-08-17 | 安阳钢铁股份有限公司 | New method for using oxygen pipeline and spherical tank |
| CN102295960A (en) * | 2011-06-21 | 2011-12-28 | 杭州中泰深冷技术股份有限公司 | Apparatus and method for purifying synthetic gas with liquid nitrogen |
| CN104019629A (en) * | 2014-05-14 | 2014-09-03 | 中国海洋石油总公司 | Air separation method capable of being matched with cold energy supply in receiving station |
| CN113154796A (en) * | 2021-03-23 | 2021-07-23 | 金川集团股份有限公司 | Variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recycling oxygen-nitrogen resources |
| CN113368650A (en) * | 2021-05-18 | 2021-09-10 | 重庆宏大化工科技有限公司 | Waste gas purification and recovery treatment device and method for hydrogen peroxide production |
-
2002
- 2002-02-07 CN CN 02100593 patent/CN1239875C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102155626A (en) * | 2010-12-30 | 2011-08-17 | 安阳钢铁股份有限公司 | New method for using oxygen pipeline and spherical tank |
| CN102155626B (en) * | 2010-12-30 | 2012-10-24 | 安阳钢铁股份有限公司 | New method for using oxygen pipeline and spherical tank |
| CN102295960A (en) * | 2011-06-21 | 2011-12-28 | 杭州中泰深冷技术股份有限公司 | Apparatus and method for purifying synthetic gas with liquid nitrogen |
| CN104019629A (en) * | 2014-05-14 | 2014-09-03 | 中国海洋石油总公司 | Air separation method capable of being matched with cold energy supply in receiving station |
| CN104019629B (en) * | 2014-05-14 | 2016-01-06 | 中国海洋石油总公司 | A kind of air separating method that can match with receiving station's cold energy supply |
| CN113154796A (en) * | 2021-03-23 | 2021-07-23 | 金川集团股份有限公司 | Variable multi-cycle oxygen-nitrogen cold energy utilization device and method for recycling oxygen-nitrogen resources |
| CN113368650A (en) * | 2021-05-18 | 2021-09-10 | 重庆宏大化工科技有限公司 | Waste gas purification and recovery treatment device and method for hydrogen peroxide production |
| CN113368650B (en) * | 2021-05-18 | 2023-08-15 | 重庆宏大化工科技有限公司 | Waste gas purification and recovery treatment device and method for hydrogen peroxide production |
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|---|---|
| CN1239875C (en) | 2006-02-01 |
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