CN205607022U - Produce device of high pure oxygen and high pure nitrogen - Google Patents
Produce device of high pure oxygen and high pure nitrogen Download PDFInfo
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- CN205607022U CN205607022U CN201620271263.0U CN201620271263U CN205607022U CN 205607022 U CN205607022 U CN 205607022U CN 201620271263 U CN201620271263 U CN 201620271263U CN 205607022 U CN205607022 U CN 205607022U
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Abstract
The utility model provides a produce device of high pure oxygen and high pure nitrogen, include: fractionating tower main heat exchanger (E1), subcooler (E2), high -pressure rectifying column (C1), middling pressure rectifying column (C2), low pressure rectifying column (C3), wherein, high pressure rectifying column top of the tower is provided with condensing evaporator (K1), be provided with reboiler (K2) at the bottom of the middling pressure rectification tata, its top of the tower is provided with the supplementary condensing evaporator (K4) of oxygen boosting liquid, be provided with condensing evaporator (K3) at the bottom of the low pressure rectification tata, its top of the tower is provided with condensing evaporator (K5), a plurality of valves and pipeline for each equipment more than connecting. Adopt the high pure oxygen and the high pure nitrogen are isolated to the device from the air, does the extraction percentage of the high pure nitrogen of gained reach 60 does 75%, the extraction percentage of high pure oxygen reach 70% 72%, but device widely used has good market prospect.
Description
Technical field
This utility model belongs to gas producing plant field, particularly relates to a kind of dress producing high pure oxygen and High Purity Nitrogen
Put.
Background technology
Along with the fast development of the industry such as electronics, chemical industry, high pure nitrogen, high pure oxygen demand are increased dramatically,
Generally industrial oxygen purity is 99.6%O2, and the high pure oxygen purity ＞ 99.9999%O needed for electronics industry2；
In precision electronic industries, high pure oxygen is normally used for the chemical gaseous phase deposition of silicon dioxide, or as oxidation
Source and the reactant producing high purity water；Or for dry oxidation；Or mix with carbon tetrafluoride, for plasma
Etching etc..
Current commonly used liquid oxygen is that raw material carries out producing of high pure oxygen, but its extraction ratio is on the low side；And use krypton
In xenon raw process flow process, through once, secondarily purified after oxygen, purity reaches 99.5%～99.99%,
It is the splendid raw material of high purity oxygen, is characterized in that yield is big, purity is high, and the rough releasing oxygen of krypton xenon comes
Source becomes the reason limiting high-purity fluid oxygen yield more at least.
Major gaseous component in air is that nitrogen and oxygen, nitrogen and oxygen purity are respectively 78.12%
With 20.95%, and air is ubiquitous as low-cost resource, is therefore directly produced high-purity by separation air
Nitrogen and high purity oxygen gas are the easiest and economic methods.Therefore, develop a set of being suitable to separate from air
Go out the device of high pure oxygen and High Purity Nitrogen, become one of study hotspot of current Chemical R & D personnel.
Utility model content
This utility model is intended to overcome many disadvantages present in above-mentioned prior art, and provides a kind of from air
Isolate the device of high pure oxygen and High Purity Nitrogen, meet the field such as precision electronic industries, biological medicine uses high-purity
Oxygen and the demand of High Purity Nitrogen.
Therefore, this utility model provides a kind of device producing high pure oxygen and High Purity Nitrogen, specifically includes:
Fractionating column main heat exchanger E1, subcooler E2, high-pressure rectification tower C1, middle pressure rectifying column C2, low pressure essence
Evaporating tower C3, wherein, described high-pressure rectification column overhead is provided with condenser/evaporator K1；Medium pressure rectifying tower
The end, is provided with reboiler K2, and its tower top is provided with oxygen-rich liquid auxiliary condenser/evaporator K4；Described low-pressure distillation tower
Being provided with condenser/evaporator K3 at the bottom of tower, its tower top is provided with condenser/evaporator K5；Some valves and pipeline, use
Each equipment more than connecting, to implement following technological process:
Dried for purification air is cooled to saturation in fractionating column main heat exchanger E1, a part of saturated
Air enters high-pressure rectification tower C1 tower reactor, is separated into high pressure nitrogen and oxygen-enriched liquid air in high-pressure rectification tower C1；
Another part saturated air is pressed in rectifying column reboiler K2 in entering and is condensed into liquid air；Described liquid air and described richness
After the mixing of oxygen liquid air, enter in high-pressure rectification tower condenser/evaporator K1 and flash to gaseous state, enter back into middle pressure rectification
Tower tower reactor；The nitrogen separated by high-pressure rectification tower C1 is sent in high-pressure rectification tower condenser/evaporator K1 cold
Congealing into for liquid nitrogen, a part of liquid nitrogen is as high-pressure rectification tower backflow, and another part liquid nitrogen is through subcooler E2 mistake
After cold, entrance is pressed rectifying column C2 top as middle pressure rectifier column reflux liquid；High-pressure rectification tower condenser/evaporator
The oxygen rich air that K1 evaporates respectively enters middle pressure rectifying column C2 and carries out rectification, is separated into medium pressure nitrogen gas and oxygen-enriched
Liquid；
Therefrom extract the described oxygen-rich liquid rich in low boiling hydrocarbon out bottom pressure rectifying column C2, auxiliary subsequently into oxygen-rich liquid
Help condenser/evaporator K4；In described oxygen-rich liquid auxiliary condenser/evaporator K4, oxygen-rich liquid is evaporated into oxygen-enriched
Gas, exports after re-heat；
Therefrom pressure rectifying column C2 tower top extracts medium pressure nitrogen out, and it is cold that medium pressure nitrogen enters low-pressure distillation tower
Solidifying vaporizer K3, then it is condensed into middle hydraulic fluid nitrogen, a part of medium pressure liquid nitrogen presses rectifying column C2 tower in returning
Top, as the backflow pressing rectifying column in this；Another part medium pressure liquid nitrogen throttles to 0.01～0.03MPa
Evaporated, after evaporation with the dirty nitrogen heat exchange in the condenser/evaporator K5 of low-pressure distillation tower C3 tower top afterwards
Low-pressure nitrogen is after subcooler E2, main heat exchanger E1 re-heat, as high pure nitrogen output of products；And condense
Liquid nitrogen fraction as the backflow of low-pressure distillation tower (C3)；
Therefrom extract the oxygen-rich liquid without low boiling hydrocarbon out in the middle part of pressure rectifying column C2, after subcooler is supercool, enter
Low-pressure distillation tower C3 tower top is as the backflow of this low-pressure distillation tower；The described oxygen-rich liquid without low boiling hydrocarbon exists
In low-pressure distillation tower C3 after rectification, obtain high-purity fluid oxygen product in this low-pressure distillation tower tower reactor.
Preferably, the device of the high pure oxygen of described production and High Purity Nitrogen also includes: from medium pressure rectifying column C2 tower
Top is extracted medium pressure nitrogen out and is entered the middle hydraulic fluid nitrogen place being condensed into after low-pressure distillation tower condenser/evaporator K3
Pipeline, be divided into three tunnels: during hydraulic fluid nitrogen returns in first via pipelined, press rectifying column C2 tower top；Second
In the pipelined of road, hydraulic fluid nitrogen directly exports as liquid nitrogen product；In first via pipelined, hydraulic fluid indole flow to
With the dirty nitrogen heat exchange in the condenser/evaporator K5 of low-pressure distillation tower C3 tower top and quilt after 0.01～0.03MPa
Evaporation, the low-pressure nitrogen after evaporation, after subcooler E2, main heat exchanger E1 re-heat, produces as high pure nitrogen
Product export；And the liquid nitrogen fraction condensed is as the backflow of low-pressure distillation tower (C3).
It is further preferred that the device of the high pure oxygen of described production and High Purity Nitrogen also includes:
Nitrogen compressor CP2, turbo-expander ET01 and pressurized end Z01 thereof, water cooler E3, and
Described low-pressure nitrogen pipeline after subcooler E2, main heat exchanger E1 re-heat, is divided into two-way:
Wherein, first via pipelined low-pressure nitrogen is directly as high pure nitrogen output of products；
Wherein, the second tunnel pipelined low-pressure nitrogen enters nitrogen compressor CP2 and is compressed, then carries out cold
But, supercharging is carried out subsequently into turbo-expander ET01 pressurized end Z01, then cold in water cooler E3
But, subsequently enter in described fractionating column main heat exchanger E1 and cool down further, then from described fractionating column main heat exchanger
The middle part of E1 is extracted out, after entering described turbo-expander ET01 expansion, returns described fractionating column main heat exchanger
E1 re-heat, is incorporated into described low-pressure nitrogen pipeline after subcooler E2, main heat exchanger E1 re-heat afterwards.
It is further preferred that the pipeline that above-mentioned low-pressure nitrogen is after subcooler E2, main heat exchanger E1 re-heat
Suction inlet for described nitrogen compressor CP2.
Preferably, the device of the high pure oxygen of described production and High Purity Nitrogen also includes:
Turbo-expander ET01 and pressurized end Z01 thereof, water cooler E3, and described purification is dried
Air is cooled to the pipeline before saturation in fractionating column main heat exchanger E1, is divided into two-way:
Wherein, the dried air of first via pipelined purification is directly entered fractionating column main heat exchanger E1；
Wherein, the second tunnel dried air of pipelined purification enters turbo-expander ET01 pressurized end Z01
Carry out supercharging, then cool down in water cooler E3, subsequently enter in described fractionating column main heat exchanger E1
One step cooling, then extract out from the middle part of described fractionating column main heat exchanger E1, enter described turbo-expander ET01
After expansion, it is back to described fractionating column main heat exchanger E1 and carries out re-heat；Through described fractionating column main heat exchanger E1
The low-pressure air of output, after air booster supercharging, is incorporated into as the air that backflows before being divided into two-way
Conveying the dried air of described purification pipeline.
Preferably, in the device of the high pure oxygen of described production and High Purity Nitrogen: the operation pressure of described high-pressure rectification tower C1
Power is 0.8～1.3MPa, and the operation pressure of medium pressure rectifying column C2 is 0.35～0.6MPa, described low pressure
The operation pressure of rectifying column C3 is 0.02～0.15MPa.Aforesaid operations pressure preferably in the range of, described in
It is 0.5MPa that pressure rectifying column C2 most preferably operates pressure.
Use device described in the utility model prepare high pure oxygen in O2Purity >=99.9999%, described high-purity
N in nitrogen2Purity >=99.999%.Visible, obtained high pure oxygen and/or High Purity Nitrogen have all reached relevant state
Family's standard.
Compared with prior art, this utility model has the advantage that
(1) Traditional high purity oxygen mainly purifies from industry oxygen (99.5%), it is generally required to 2～3
Rectifying column, removes the high boiling component (methane, krypton, xenon, nitrous oxide etc.) in industry oxygen, then respectively
Going the argon component in deoxygenation, this utility model is on the middle pressure tower bottom of rectifying tower of High Purity Nitrogen product producing band pressure
Side's at least one equilibrium stage extraction is substantially free of the oxygen-rich liquid of methane as raw material, methane contained therein, krypton,
The high boiling component content such as xenon are ppb level, and the extraction ratio of nitrogen does not reduce simultaneously；
(2) reclaim while this utility model can realize High Purity Nitrogen and high pure oxygen, wherein, the extraction of High Purity Nitrogen
Rate reaches 60-75%, extraction rate reached 70%-72% of high pure oxygen；
(3) high pure oxygen product is various informative, and the high pure oxygen product of production can be gas, it is possible to produce for liquid oxygen
Product, are delivered to liquid storage groove storage；
(4) the low pure liquid oxygen of part is discharged (containing about 50-70% oxygen, containing methane in medium pressure rectifier bottoms
About 100-500ppm, surplus is krypton, xenon, nitrous oxide etc.) make the content of hydrocarbon in medium pressure rectifying column drop
Low, improve the safety of equipment.
(5) device provided by the utility model is used to produce high pure oxygen and/or High Purity Nitrogen, highly effective, and
With air as raw material, the most economical；Products obtained therefrom is safe and reliable, the available extensively application of this device, has good
Good market prospect.
Accompanying drawing explanation
Fig. 1 is the structure chart of an embodiment 1 of device described in the utility model；
Wherein: 101 is the dried air of the purification in main line, and 102,201 is that the purification in branch road is dried
After air, 103 be from fractionating column main heat exchanger output saturated air, 104,105 be from 103 shunt
Two parts saturated air, 106,107 is liquid air, and 202,203,204 are the air after supercharging, 205,
206 is the low-pressure air after expanding, and 300 is high pressure nitrogen, and 301,302,303 is high-pressure liquid nitrogen, 304
For middle hydraulic fluid nitrogen, 401,402,404,407 is medium pressure nitrogen gas, 403,405,406,410,302b
For middle hydraulic fluid nitrogen, 411 is low pressure liquid nitrogen, and 412,413,414 is low-pressure nitrogen, 501,502,503
For liquid air, 504 is oxygen rich air, 601,602 be in the middle part of middle pressure rectifying column extract out oxygen-rich liquid, 604,605,
607,608,609 being dirty nitrogen, 606 be the liquid nitrogen fraction of condensation, 603 is oxygen-rich liquid 602 and liquid nitrogen fraction 606
Mixture, 701 is high-purity liquid oxygen, 901,902,903 be middle pressure tower bottom of rectifying tower extract out oxygen-rich liquid,
904,906 is the oxygen rich air that middle pressure rectifying column auxiliary condenser/evaporator K4 evaporates, and E1 is main heat exchanger, E2
For subcooler, E3 is water cooler, and K1 is high-pressure rectification tower condenser/evaporator, K2 be middle pressure rectifying column again
Boiling device, K3 is low-pressure distillation tower tower reactor vaporizer, and K4 is that oxygen-rich liquid assists condenser/evaporator, and K5 is low pressure
The condenser/evaporator of rectifying column C3 tower top, C1 is high-pressure rectification tower, and C2 is middle pressure rectifying column, and C3 is low
Pressure rectifying column, ET01 is turbo-expander, Z01 be connect turbo-expander supercharger, V501, V502,
V503, V513, V514, V515 are choke valve.
Fig. 2 is the structure chart of an embodiment 2 of device described in the utility model；
Wherein: 101 is the dried air of the purification in main line, 103 is satisfying from the output of fractionating column main heat exchanger
And air, 104,105 is two parts saturated air from 103 shuntings, and 106,107 is liquid air, 207,
201 is the nitrogen after nitrogen compressor CP2 compresses, and 202,203,204 are the nitrogen after supercharging,
205,206 is the low-pressure nitrogen after expanding, and 415 is the low-pressure nitrogen supplementing nitrogen compressor CP2,300
For high pressure nitrogen, 301,302,303 is high-pressure liquid nitrogen, and 304 is middle hydraulic fluid nitrogen, 401,402,404,
407 is medium pressure nitrogen gas, 403,405,406,410,302b be middle hydraulic fluid nitrogen, 411 is low pressure liquid nitrogen,
412,413,414 is low-pressure nitrogen, and 501,502,503 is liquid air, and 504 is oxygen rich air, 601,
602 be in the middle part of middle pressure rectifying column extract out oxygen-rich liquid, 604,605,607,608,609 be dirt nitrogen, 606
For the liquid nitrogen fraction of condensation, 603 is the mixture of oxygen-rich liquid 602 and liquid nitrogen fraction 606, and 701 is high-purity liquid oxygen,
901,902,903 is the oxygen-rich liquid that middle pressure tower bottom of rectifying tower is extracted out, and 904,906 is middle pressure rectifying column auxiliary
The oxygen rich air of condenser/evaporator K4 evaporation, E1 is main heat exchanger, and E2 is subcooler, and E3, E4 are water-cooled
But device, K1 is high-pressure rectification tower condenser/evaporator, and K2 is middle pressure rectifying column reboiler, and K3 is low-pressure distillation
Tower tower reactor vaporizer, K4 is that oxygen-rich liquid assists condenser/evaporator, and K5 is the condensation of low-pressure distillation tower C3 tower top
Vaporizer, C1 is high-pressure rectification tower, and C2 is middle pressure rectifying column, and C3 is low-pressure distillation tower, and ET01 is
Flat decompressor, Z01 be connect turbo-expander supercharger, CP2 is nitrogen compressor, V501, V502,
V503, V513, V514, V515 are choke valve.
Detailed description of the invention
This utility model provides a kind of device producing high pure oxygen and High Purity Nitrogen, specifically includes:
Fractionating column main heat exchanger E1, subcooler E2, high-pressure rectification tower C1, middle pressure rectifying column C2, low pressure essence
Evaporating tower C3, wherein, described high-pressure rectification column overhead is provided with condenser/evaporator K1；Medium pressure rectifying tower
The end, is provided with reboiler K2, and its tower top is provided with oxygen-rich liquid auxiliary condenser/evaporator K4；Described low-pressure distillation tower
Being provided with condenser/evaporator K3 at the bottom of tower, its tower top is provided with condenser/evaporator K5；Some valves and pipeline, use
Each equipment more than connecting, to implement following technological process:
Dried for purification air is cooled to saturation in fractionating column main heat exchanger E1, a part of saturated
Air enters high-pressure rectification tower C1 tower reactor, is separated into high pressure nitrogen and oxygen-enriched liquid air in high-pressure rectification tower C1；
Another part saturated air is pressed in rectifying column reboiler K2 in entering and is condensed into liquid air；Described liquid air and described richness
After the mixing of oxygen liquid air, enter in high-pressure rectification tower condenser/evaporator K1 and flash to gaseous state, enter back into middle pressure rectification
Tower tower reactor；The nitrogen separated by high-pressure rectification tower C1 is sent in high-pressure rectification tower condenser/evaporator K1 cold
Congealing into for liquid nitrogen, a part of liquid nitrogen is as high-pressure rectification tower backflow, and another part liquid nitrogen is through subcooler E2 mistake
After cold, entrance is pressed rectifying column C2 top as middle pressure rectifier column reflux liquid；High-pressure rectification tower condenser/evaporator
The oxygen rich air that K1 evaporates respectively enters middle pressure rectifying column C2 and carries out rectification, is separated into medium pressure nitrogen gas and oxygen-enriched
Liquid；
Therefrom extract the described oxygen-rich liquid rich in low boiling hydrocarbon out bottom pressure rectifying column C2, auxiliary subsequently into oxygen-rich liquid
Help condenser/evaporator K4；In described oxygen-rich liquid auxiliary condenser/evaporator K4, oxygen-rich liquid is evaporated into oxygen-enriched
Gas, exports after re-heat；
Therefrom pressure rectifying column C2 tower top extracts medium pressure nitrogen out, and it is cold that medium pressure nitrogen enters low-pressure distillation tower
Solidifying vaporizer K3, then it is condensed into middle hydraulic fluid nitrogen, a part of medium pressure liquid nitrogen presses rectifying column C2 tower in returning
Top, as the backflow pressing rectifying column in this；Another part medium pressure liquid nitrogen throttles to 0.01～0.03MPa
Evaporated, after evaporation with the dirty nitrogen heat exchange in the condenser/evaporator K5 of low-pressure distillation tower C3 tower top afterwards
Low-pressure nitrogen is after subcooler E2, main heat exchanger E1 re-heat, as high pure nitrogen output of products；And condense
Liquid nitrogen fraction as the backflow of low-pressure distillation tower C3；
Therefrom extract the oxygen-rich liquid without low boiling hydrocarbon out in the middle part of pressure rectifying column C2, after subcooler is supercool, enter
Low-pressure distillation tower C3 tower top is as the backflow of this low-pressure distillation tower；The described oxygen-rich liquid without low boiling hydrocarbon exists
In low-pressure distillation tower C3 after rectification, obtain high-purity fluid oxygen product in this low-pressure distillation tower tower reactor.
In a preferred embodiment, the device of the high pure oxygen of described production and High Purity Nitrogen also includes: from medium pressure
Rectifying column C2 tower top is condensed into after extracting medium pressure nitrogen entrance low-pressure distillation tower condenser/evaporator K3 out
The pipeline at middle hydraulic fluid nitrogen place, is divided into three tunnels: press rectifying column during hydraulic fluid nitrogen returns in first via pipelined
C2 tower top；In second tunnel pipelined, hydraulic fluid nitrogen directly exports as liquid nitrogen product；In first via pipelined
Hydraulic fluid indole flow to after 0.01～0.03MPa with the dirt in the condenser/evaporator K5 of low-pressure distillation tower C3 tower top
Nitrogen heat exchange and evaporated, the low-pressure nitrogen after evaporation after subcooler E2, main heat exchanger E1 re-heat, make
For high pure nitrogen output of products；And the liquid nitrogen fraction condensed is as the backflow of low-pressure distillation tower C3.
In a further preferred embodiment, the device of the high pure oxygen of described production and High Purity Nitrogen also includes:
Nitrogen compressor CP2, turbo-expander ET01 and pressurized end Z01 thereof, water cooler E3, and
Described low-pressure nitrogen pipeline after subcooler E2, main heat exchanger E1 re-heat, is divided into two-way:
Wherein, first via pipelined low-pressure nitrogen is directly as high pure nitrogen output of products；
Wherein, the second tunnel pipelined low-pressure nitrogen enters nitrogen compressor CP2 and is compressed, then carries out cold
But, carrying out supercharging subsequently into turbo-expander ET01 pressurized end Z01, the most water cooled but device E3 is carried out
Cooling, subsequently enters in described fractionating column main heat exchanger E1 and cools down further, then from described fractionating column main heat exchange
The middle part of device E1 is extracted out, after entering described turbo-expander ET01 expansion, returns described fractionating column main heat exchange
Device E1 re-heat, is incorporated into described low-pressure nitrogen pipeline after subcooler E2, main heat exchanger E1 re-heat afterwards.
In one further preferred embodiment, above-mentioned low-pressure nitrogen is through subcooler E2, main heat exchanger E1
Pipeline after re-heat is the suction inlet of described nitrogen compressor CP2.
In a preferred embodiment, the device of the high pure oxygen of described production and High Purity Nitrogen also includes:
Turbo-expander ET01 and pressurized end Z01 thereof, water cooler E3, and described purification is dried
Air is cooled to the pipeline before saturation in fractionating column main heat exchanger E1, is divided into two-way:
Wherein, the dried air of first via pipelined purification is directly entered fractionating column main heat exchanger E1；
Wherein, the second tunnel dried air of pipelined purification enters turbo-expander ET01 pressurized end Z01
Carry out supercharging, then cool down in water cooler E3, subsequently enter in described fractionating column main heat exchanger E1
One step cooling, then extract out from the middle part of described fractionating column main heat exchanger E1, enter described turbo-expander ET01
After expansion, it is back to described fractionating column main heat exchanger E1 and carries out re-heat；Through described fractionating column main heat exchanger E1
The low-pressure air of output, after air booster supercharging, is incorporated into as the air that backflows before being divided into two-way
Conveying the dried air of described purification pipeline.
In a preferred embodiment, in the device of the high pure oxygen of described production and High Purity Nitrogen: described high-pressure rectification tower
The operation pressure of C1 is 0.8～1.3MPa, and the operation pressure of medium pressure rectifying column C2 is 0.35～0.6MPa,
The operation pressure of described low-pressure distillation tower C3 is 0.02～0.15MPa.In the range of aforesaid operations pressure is preferred,
It is 0.5MPa that medium pressure rectifying column C2 most preferably operates pressure.
Below in conjunction with detailed description of the invention, this utility model is further elaborated, but this utility model is not limited to
Following example.
Embodiment 1
Device as shown in Figure 1 is used to produce high pure oxygen and High Purity Nitrogen:
By dried for purification air 101 (3350NM3/ h, 0.96MPa) air 206 merges with backflowing,
After merging, described purification dried air total flow is 7750NM3/ h, and in fractionating column main heat exchanger E1
Before being cooled to saturation, it is divided into two strands:
Wherein one 102 is directly entered fractionating column main heat exchanger E1；
Wherein another stock 201 (4400NM3/ h, 0.96MPa) enter turbo-expander ET01 pressurized end Z01
Obtain 202 after being pressurized to 1.32MPa, then in water cooler E3, be cooled to 40 DEG C, subsequently enter fractionating column master
Heat exchanger E1 is cooled to-122 DEG C, extracts 204 out, and enter described turbo-expander ET01 in the middle part of main heat exchanger
It is expanded to 0.025MPa, obtains 205, return again to described fractionating column main heat exchanger E1 re-heat to 32 DEG C,
Obtain 206；Wherein, the cold that described turbo-expander produces maintains device cold balancing.Through described fractionating column
The low-pressure air 206 of main heat exchanger E1 output, after air booster is pressurized to 0.96MPa, as returning
Stream air is incorporated into the Trunk Line of the dried air of purification 101, and 101 on this Trunk Line are not also divided into two
Stock；
Above-mentioned 102 (3350NM3/ h, 0.96MPa) in fractionating column main heat exchanger E1, it is cooled to saturated shape
State 103；Then, 103 saturated air 104 and saturated air 105 two parts are split into, wherein:
Saturated air 104 (2950NM3/ h) enter high-pressure rectification tower C1 tower reactor, at this high-pressure rectification tower C1
In be separated into high pressure nitrogen 300 and oxygen-enriched liquid air 501；
Saturated air 105 (400NM3/ h) enter in press in rectifying column reboiler K2 and be condensed into liquid air 106；
After described liquid air 106 mixes with the described oxygen-enriched liquid air 501 from high-pressure rectification tower, obtain 503, so
Rear entrance high-pressure rectification tower condenser/evaporator K1 flashes to gaseous state 504, enters back into middle pressure rectifying column C2 tower reactor；
The nitrogen 404 that high-pressure rectification tower C1 separates is sent in high-pressure rectification tower condenser/evaporator K1 and be condensed into
For liquid nitrogen 405, a part of liquid nitrogen is as high-pressure rectification tower backflow, another part liquid nitrogen (1000NM3/h)
Cross through subcooler E2 and be cooled to-181 DEG C, entrance is pressed rectifying column C2 top as middle pressure rectifier column reflux liquid；High
The oxygen rich air 504 that pressure tower condenser/evaporator K1 evaporates respectively enters middle pressure rectifying column C2 and carries out rectification, its
In, the operation pressure pressing rectifying column C2 in this is 0.5MPa, is separated into medium pressure nitrogen gas 401 and richness
Oxygen liquid 901.
Press from this bottom rectifying column C2 and extract the described oxygen-rich liquid 901 (160NM rich in low boiling hydrocarbon out3/ h),
Condenser/evaporator K4 is assisted subsequently into oxygen-rich liquid；In described oxygen-rich liquid auxiliary condenser/evaporator K4, oxygen-enriched
Liquid is evaporated into oxygen rich air 904, exports 906 after re-heat；
Therefrom pressure rectifying column C2 tower top extracts medium pressure nitrogen 401 (2840NM out3/ h), medium pressure nitrogen
Gas enters low-pressure distillation tower condenser/evaporator K3, then is condensed into middle hydraulic fluid nitrogen 405, a part of medium pressure liquid
Nitrogen 405 presses rectifying column C2 tower top, as the backflow pressing rectifying column in this in returning；In described in another part
Hydraulic fluid nitrogen (1880NM3/ h) throttle to 0.03MPa the condenser/evaporator with low-pressure distillation tower C3 tower top
Dirty nitrogen heat exchange in K5 and evaporated, the low-pressure nitrogen after evaporation is multiple through subcooler E2, main heat exchanger E1
After heat, exporting as high pure nitrogen product 414, i.e. low-pressure nitrogen 414, its yield is 1880NM3/ h,
Wherein as the O of foreign gas2Content≤3pppm, pressure 0.01MPa；And the liquid nitrogen fraction condensed is as low pressure
The backflow of rectifying column C3；
Therefrom extract the oxygen-rich liquid (1300NM without low boiling hydrocarbon out in the middle part of pressure rectifying column C23/ h), passed through
The low-pressure distillation tower C3 tower top backflow 603 as this low-pressure distillation tower is entered after cooler is supercool；Described do not contain
The oxygen-rich liquid of low boiling hydrocarbon after rectification, obtains O in this low-pressure distillation tower tower reactor in low-pressure distillation tower C32Purity
The high-purity fluid oxygen product 701 (500NM of >=99.9999%3/h)。
Embodiment 2
Device as shown in Figure 2 is used to produce high pure oxygen and High Purity Nitrogen:
By dried for purification air 101 (3350NM3/ h, 0.96MPa) at fractionating column main heat exchanger E1
In be cooled to saturation 103, a part of saturated air 104 (2950NM3/ h) enter high-pressure rectification tower
C1 tower reactor, is separated into high pressure nitrogen 300 and oxygen-enriched liquid air 501 in high-pressure rectification tower C1；Another part
Saturated air 105 (400NM3/ h) enter in press in rectifying column reboiler K2 and be condensed into liquid air 106, liquid air
106 mix with the oxygen-enriched liquid air 501 of high pressure tower reactor after 503, enter in high-pressure rectification tower condenser/evaporator K1
Flash to gaseous state 504, enter back into middle pressure tower bottom of rectifying tower；The nitrogen 404 that high-pressure rectification tower C1 is separated
Sending into high-pressure rectification tower condenser/evaporator K1 condensation and become liquid nitrogen 405, a part of liquid nitrogen therein is as high pressure
Rectifier column reflux liquid；Another branch liquid nitrogen (1000NM therein3/ h) cross through subcooler E2 and to be cooled to-181 DEG C,
Entrance is pressed rectifying column C2 top evaporate as middle pressure rectifier column reflux liquid, high-pressure rectification tower condenser/evaporator K1
The oxygen rich air 504 gone out respectively enters middle pressure rectifying column C2 and carries out rectification, wherein, presses rectifying column C2's in this
Operation pressure is 0.5MPa, is separated into medium pressure nitrogen gas 401 and oxygen-rich liquid 901.
Therefrom extract the described oxygen-rich liquid 901 (160NM rich in low boiling hydrocarbon out bottom pressure rectifying column C23/ h),
Condenser/evaporator K4 is assisted subsequently into oxygen-rich liquid；In described oxygen-rich liquid auxiliary condenser/evaporator K4, oxygen-enriched
Liquid is evaporated into oxygen rich air 904, exports 906 after re-heat；
Therefrom pressure rectifying column C2 tower top extracts medium pressure nitrogen 401 (2840NM out3/ h), medium pressure nitrogen
Gas enters low-pressure distillation tower condenser/evaporator K3, then is condensed into middle hydraulic fluid nitrogen 404, described in a portion in
Hydraulic fluid nitrogen presses rectifying column C2 tower top, as the backflow pressing rectifying column in this in returning；Wherein in another part
Hydraulic fluid nitrogen 405 (1880NM3/ h) throttle to 0.01MPa, the condensation with low-pressure distillation tower C3 tower top is steamed
Sending out dirty nitrogen 609 heat exchange in device K5 and evaporate, the low-pressure nitrogen after evaporation is through subcooler E2, main heat exchanger
After E1 re-heat, exporting as high pure nitrogen product 414, i.e. low-pressure nitrogen 414, its yield is 1880NM3/ h,
Wherein as the O of foreign gas2Content≤3pppm, pressure 0.01MPa；And the liquid nitrogen fraction condensed is as low pressure
The backflow of rectifying column C3；
Therefrom extract the oxygen-rich liquid 601 (1300NM without low boiling hydrocarbon out in the middle part of pressure rectifying column C23/ h), warp
After subcooler is supercool, enter the low-pressure distillation tower C3 tower top backflow 603 as this low-pressure distillation tower；Described
Oxygen-rich liquid without low boiling hydrocarbon after rectification, obtains O in this low-pressure distillation tower tower reactor in low-pressure distillation tower C32
The high-purity fluid oxygen product 701 (500NM of purity >=99.9999%3/h)。
Additionally, from main heat exchanger E1 output low-pressure nitrogen 414 be divided into two strands, wherein one as it has been described above,
Directly as high pure nitrogen output of products；And another strand of low-pressure nitrogen 414 mixes with 206, obtain 207
(4100NM3/ h, 0.01MPa, 32 DEG C), enter nitrogen compressor CP2, be compressed to 0.96MPa, then
Being cooled to less than 40 DEG C, the pressurized end Z01 subsequently into turbo-expander ET01 is pressurized to 1.32MPa,
Obtain 202, in water cooler E3, be cooled to 40 DEG C afterwards, subsequently enter described fractionating column main heat exchanger E1
It is cooled to-122 DEG C, obtains 204；Extract out from the middle part of main heat exchanger E1 again, enter turbo-expander ET01 swollen
Swollen to 0.025MPa, obtain 205, be then back to described fractionating column main heat exchanger E1 re-heat to 32 DEG C, obtain 206,
This 206 is incorporated into described another strand of low-pressure nitrogen；Wherein, the cold that decompressor produces maintains device cold to put down
Weighing apparatus.
Above specific embodiment of the utility model is described in detail, but it has been intended only as example, this reality
It is not restricted to particular embodiments described above with novel.To those skilled in the art, any to this
The equivalent modifications that utility model is carried out and replacement are the most all among category of the present utility model.Therefore, without departing from
The impartial conversion made under spirit and scope of the present utility model and amendment, all should contain at model of the present utility model
In enclosing.
Claims (6)
1. the device producing high pure oxygen and High Purity Nitrogen, it is characterised in that including: fractionating column main heat exchanger (E1),
Subcooler (E2), high-pressure rectification tower (C1), middle pressure rectifying column (C2), low-pressure distillation tower (C3), wherein,
Described high-pressure rectification column overhead is provided with condenser/evaporator (K1)；It is provided with at the bottom of medium pressure rectifying tower and boils again
Device (K2), its tower top is provided with oxygen-rich liquid auxiliary condenser/evaporator (K4)；Set at the bottom of described low-pressure distillation tower tower
Being equipped with condenser/evaporator (K3), its tower top is provided with condenser/evaporator (K5)；Some valves and pipeline, use
Each equipment more than connecting, to implement following technological process:
Dried for purification air is cooled to saturation in fractionating column main heat exchanger (E1), a part
Saturated air enters high-pressure rectification tower (C1) tower reactor, is separated into high pressure nitrogen in high-pressure rectification tower (C1)
And oxygen-enriched liquid air；Another part saturated air is pressed in rectifying column reboiler (K2) in entering and is condensed into liquid air；
After described liquid air mixes with described oxygen-enriched liquid air, enter in high-pressure rectification tower condenser/evaporator (K1) and flash to
Gaseous state, enters back into middle pressure tower bottom of rectifying tower；The nitrogen separated by high-pressure rectification tower (C1) sends into high pressure
Condensation becomes liquid nitrogen in rectifying column condenser/evaporator (K1), a part of liquid nitrogen as high-pressure rectification tower backflow,
Another part liquid nitrogen, after subcooler (E2) is supercool, presses rectifying column (C2) top as middle pressure essence in entrance
Evaporate tower backflow；The oxygen rich air that high-pressure rectification tower condenser/evaporator (K1) evaporates respectively enters middle pressure rectification
Tower (C2) carries out rectification, is separated into medium pressure nitrogen gas and oxygen-rich liquid；
Rectifying column (C2) bottom is therefrom pressed to extract the described oxygen-rich liquid rich in low boiling hydrocarbon out, subsequently into oxygen-enriched
Liquid auxiliary condenser/evaporator (K4)；In described oxygen-rich liquid auxiliary condenser/evaporator (K4), oxygen-rich liquid is steamed
Send out into oxygen rich air, export after re-heat；
Therefrom pressing rectifying column (C2) tower top to extract medium pressure nitrogen out, medium pressure nitrogen enters low-pressure distillation
Tower condenser/evaporator (K3), then it is condensed into middle hydraulic fluid nitrogen, a part of medium pressure liquid nitrogen presses rectifying column in returning
(C2) tower top, as the backflow pressing rectifying column in this；Another part medium pressure liquid nitrogen throttles extremely
Change with the dirty nitrogen in the condenser/evaporator (K5) of low-pressure distillation tower (C3) tower top after 0.01～0.03MPa
Heat and evaporated, the low-pressure nitrogen after evaporation after subcooler (E2), main heat exchanger (E1) re-heat, as
High pure nitrogen output of products；And the liquid nitrogen fraction condensed is as the backflow of low-pressure distillation tower (C3)；
Rectifying column (C2) middle part is therefrom pressed to extract the oxygen-rich liquid without low boiling hydrocarbon out, after subcooler is supercool,
Enter low-pressure distillation tower (C3) tower top backflow as this low-pressure distillation tower；Described without low boiling hydrocarbon
Oxygen-rich liquid after rectification, obtains high-purity fluid oxygen product in this low-pressure distillation tower tower reactor in low-pressure distillation tower (C3).
Device the most according to claim 1, it is characterised in that also include: from medium pressure rectifying column (C2)
Tower top is extracted medium pressure nitrogen out and is entered the middle hydraulic fluid being condensed into after low-pressure distillation tower condenser/evaporator (K3)
The pipeline at nitrogen place, is divided into three tunnels: press rectifying column (C2) during hydraulic fluid nitrogen returns in first via pipelined
Tower top；In second tunnel pipelined, hydraulic fluid nitrogen directly exports as liquid nitrogen product；Hydraulic fluid in first via pipelined
Indole flow to after 0.01～0.03MPa with in the condenser/evaporator (K5) of low-pressure distillation tower (C3) tower top
Dirty nitrogen heat exchange and evaporated, the low-pressure nitrogen after evaporation is through subcooler (E2), main heat exchanger (E1) re-heat
After, as high pure nitrogen output of products；And the liquid nitrogen fraction condensed is as the backflow of low-pressure distillation tower (C3).
Device the most according to claim 1 and 2, it is characterised in that also include: nitrogen compressor (CP2),
Turbo-expander (ET01) and pressurized end (Z01) thereof, water cooler (E3), and described low-pressure nitrogen
Pipeline after subcooler (E2), main heat exchanger (E1) re-heat, is divided into two-way:
Wherein, first via pipelined low-pressure nitrogen is directly as high pure nitrogen output of products；
Wherein, the second tunnel pipelined low-pressure nitrogen enters nitrogen compressor (CP2) and is compressed, then carries out
Cooling, carries out supercharging, then at water cooler subsequently into turbo-expander (ET01) pressurized end (Z01)
(E3) in, cooling, subsequently enters in described fractionating column main heat exchanger (E1) and cools down further, then from described
The middle part of fractionating column main heat exchanger (E1) is extracted out, after entering described turbo-expander (ET01) expansion, returns
Return the re-heat of described fractionating column main heat exchanger (E1), be incorporated into afterwards described low-pressure nitrogen through subcooler (E2),
Pipeline after main heat exchanger (E1) re-heat.
Device the most according to claim 3, it is characterised in that described low-pressure nitrogen is through subcooler (E2), master
The suction inlet that pipeline is described nitrogen compressor (CP2) after heat exchanger (E1) re-heat.
Device the most according to claim 1, it is characterised in that also include: turbo-expander (ET01) and
Its pressurized end (Z01), water cooler (E3), and the dried air of described purification is at fractionating column main heat exchange
Device (E1) is cooled to the pipeline before saturation, is divided into two-way:
Wherein, the dried air of first via pipelined purification is directly entered fractionating column main heat exchanger (E1)；
Wherein, the second tunnel dried air of pipelined purification enters turbo-expander (ET01) pressurized end
(Z01) supercharging is carried out, then cooling in water cooler (E3), subsequently enter described fractionating column main heat exchange
Device (E1) cools down further, then extracts out from the middle part of described fractionating column main heat exchanger (E1), enter institute
After stating turbo-expander (ET01) expansion, it is back to described fractionating column main heat exchanger (E1) and carries out re-heat；
Through the low-pressure air that described fractionating column main heat exchanger (E1) exports, after air booster supercharging, as
The air that backflows is incorporated into the pipeline of the conveying dried air of described purification before being divided into two-way.
Device the most according to claim 1, it is characterised in that the operation of described high-pressure rectification tower (C1)
Pressure is 0.8～1.3MPa, and the operation pressure of medium pressure rectifying column (C2) is 0.35～0.6MPa, institute
The operation pressure stating low-pressure distillation tower (C3) is 0.02～0.15MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620271263.0U CN205607022U (en) | 2016-04-01 | 2016-04-01 | Produce device of high pure oxygen and high pure nitrogen |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620271263.0U CN205607022U (en) | 2016-04-01 | 2016-04-01 | Produce device of high pure oxygen and high pure nitrogen |
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| CN201620271263.0U Expired - Fee Related CN205607022U (en) | 2016-04-01 | 2016-04-01 | Produce device of high pure oxygen and high pure nitrogen |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110207458A (en) * | 2019-07-10 | 2019-09-06 | 上海联风能源科技有限公司 | A kind of air is the high pure oxygen process units and its production method of raw material |
| CN114111218A (en) * | 2020-08-25 | 2022-03-01 | 贵州盈德气体有限公司 | Novel energy-saving process for air separation liquefaction of compressed air |
-
2016
- 2016-04-01 CN CN201620271263.0U patent/CN205607022U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110207458A (en) * | 2019-07-10 | 2019-09-06 | 上海联风能源科技有限公司 | A kind of air is the high pure oxygen process units and its production method of raw material |
| CN110207458B (en) * | 2019-07-10 | 2024-04-02 | 上海联风气体有限公司 | High-purity oxygen production device taking air as raw material and production method thereof |
| CN114111218A (en) * | 2020-08-25 | 2022-03-01 | 贵州盈德气体有限公司 | Novel energy-saving process for air separation liquefaction of compressed air |
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