CN206724574U - The device of oxygen rich gas and high pure nitrogen is produced while a kind of low energy consumption - Google Patents
The device of oxygen rich gas and high pure nitrogen is produced while a kind of low energy consumption Download PDFInfo
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- CN206724574U CN206724574U CN201720441525.8U CN201720441525U CN206724574U CN 206724574 U CN206724574 U CN 206724574U CN 201720441525 U CN201720441525 U CN 201720441525U CN 206724574 U CN206724574 U CN 206724574U
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 206
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 102
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 239000001301 oxygen Substances 0.000 title claims abstract description 72
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 72
- 239000007789 gas Substances 0.000 title claims abstract description 44
- 238000005265 energy consumption Methods 0.000 title claims description 18
- 238000000746 purification Methods 0.000 claims abstract description 18
- 238000007906 compression Methods 0.000 claims abstract description 15
- 230000006835 compression Effects 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims description 48
- 238000004891 communication Methods 0.000 claims description 46
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 26
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 230000008676 import Effects 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 21
- 238000010276 construction Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 description 13
- 229910001882 dioxygen Inorganic materials 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 239000000047 product Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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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
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure 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
- F25J3/04406—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 dual pressure main column system
- F25J3/04412—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 dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
- F25J3/04763—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
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04884—Arrangement of reboiler-condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being oxygen
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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
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/50—One fluid being oxygen
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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 utility model provides device that is a kind of while producing oxygen rich gas and high pure nitrogen, described device includes air compression system, air precooling system, sieve purification system, booster expansion turbine, main heat exchanger, rectifying column and subcooler, is connected between each equipment by pipeline.Using device of the present utility model while high pure nitrogen is produced, moreover it is possible to produce the oxygen rich gas of different purity, the oxygen rich gas can be used directly for subsequent production, reduced the repeated construction and investment of equipment, reduced production cost.
Description
Technical field
The utility model belongs to gas separating method and engineering device technique field, and in particular to is produced while a kind of low energy consumption
The device of oxygen rich gas and high pure nitrogen.
Background technology
Oxygen is current industrial important source material as combustion adjuvant, oxidant.In coal chemical industry, steel, chemical fertilizer, coloured
The fields such as smelting are widely used.Using pure oxygen or oxygen-enriched, discharge amount of exhaust gas is not only effectively reduced, can more reduce energy damage
Lose, save cost of material.
Industrial oxygen production at present mainly has two methods：Cryogenic air separation and pressure-variable adsorption.Cryogenic air separation one
As be applied in large-scale plant, have that oxygen product purity is high, and device stability is good, can by-product nitrogen and liquid oxygen, liquid simultaneously
The characteristics of byproducts such as nitrogen, liquid argon；It is less demanding that pressure-variable adsorption is mainly used in oxygen purity, the less occasion of oxygen output,
Short with the manufacturing cycle, cost is low, it is easy to operate the characteristics of.The stable performance of deep cooling separating method, nitrogen can be produced simultaneously
Feature becomes the oxygen preparation method of Large Scale Industrial Process prioritizing selection.The oxygen being prepared of deep cooling separating method is pure
Degree in many industrial processes and does not need the oxygen of this high-purity more than 99.6%, in order to meet to produce need
Ask, generally require to use the method for mixing large quantity of air into the oxygen of high-purity to be reduced to the oxygen of high-purity suitable pure
Subsequent production is entered back into after degree.This has resulted in the waste of the energy, while adds production cost.In addition, cryogenic air separation
The raw material of method is air, and its main consumption is the energy, in the case of energy growing tension, how to reduce cryogenic air point
From the energy consumption of method, it has also become it is in the urgent need to address the problem of.Therefore, in order to meet in existing industrial production to low-purity oxygen
Demand and avoid the wasting of resources, there is an urgent need to develop a kind of production technology that can prepare low-purity oxygen of low energy consumption.
Utility model content
The purpose of this utility model is the defects of presence for prior art and deficiency, there is provided is given birth to while a kind of low energy consumption
Produce the device of oxygen rich gas and high pure nitrogen.By the technical solution of the utility model, while high pure nitrogen can be obtained, go back
The oxygen rich gas for specifying purity can be obtained, the oxygen rich gas of production can be used directly for subsequent production, simplify production process,
Meanwhile the technical solution of the utility model can or else increase equipment in the case of reach conventional cryogenic air separation unit operating condition, and
And operation energy consumption is low.
The technical solution adopted in the utility model is as follows：
The utility model provides the device that oxygen rich gas and high pure nitrogen are produced while a kind of low energy consumption, described device bag
Include air compression system, air precooling system, sieve purification system, booster expansion turbine, main heat exchanger, rectifying column and mistake
Cooler；The air compression system, air precooling system and sieve purification system be the conventional air compression system in this area,
Air precooling system and sieve purification system；It is cold that the rectifying column includes Shang Ta, lower tower and master between Shang Ta, lower tower
Solidifying evaporator, the main condenser evaporator includes upper strata main condenser evaporator K1 and lower floor main condenser evaporator K2, upper strata master are cold
Solidifying to be separated between evaporator K1 and lower floor main condenser evaporator K2 with dividing plate, upper strata main condenser evaporator K1 splices with upper tower bottom
And be connected together, lower floor main condenser evaporator K2 is stitched together with lower top of tower；It is connected between each equipment by pipeline,
Its annexation is：
Air compression system is sequentially communicated with air precooling system, sieve purification system by pipeline, molecular sieve purification
The outlet of system is divided into two-way：
Connected all the way by 101 pipelines with the pressurized end air intlet of booster expansion turbine, booster expansion turbine
Pressurized end air outlet slit passes through 103 pipelines and the pressurized air inlet communication of main heat exchanger, the pressurized air outlet of main heat exchanger
Connected by 201 pipelines with the expanding end air intlet of booster expansion turbine, the expanding end air of booster expansion turbine goes out
Mouth passes through the expanded air inlet communication of 104 pipelines and upper tower；
Another way is connected by 102 pipelines with the air intlet of main heat exchanger, and the air outlet slit of main heat exchanger passes through 202 pipes
Road and lower floor main condenser evaporator K2 air side inlet communication, lower floor main condenser evaporator K2 air side outlet pass through 301
Pipeline and lower tower lower air inlet communication, lower floor main condenser evaporator K2 oxygen rich gas outlet are changed by 302 pipelines and master
The oxygen rich gas inlet communication of hot device, oxygen rich gas outlet discharge of the oxygen rich gas through main heat exchanger are collected；The height on Xia Ta tops
Pure nitrogen gas outlet is connected by 401 pipelines with upper strata main condenser evaporator K1 nitrogen side-entrance, upper strata main condenser evaporator K1
Liquid nitrogen outlet be divided into two-way after 303 pipelines, enter all the way into the liquid nitrogen inlet communication of 303A pipelines and lower tower, another way
The liquid nitrogen inlet communication of 303B pipelines and subcooler, upper strata main condenser evaporator K1 liquid oxygen-enriched outlet by 304 pipelines with
Lower floor main condenser evaporator K2 liquid oxygen-enriched inlet communication, 304 pipelines are provided with stop valve 1；Upper strata main condenser evaporator K1
High purity oxygen gas outlet pass through 305 pipelines and 302 pipeline communications, 305 pipelines are provided with stop valve 2；The poor liquid air of Xia Ta bottoms
Outlet passes through 403 pipelines and mistake by 402 pipelines and the poor liquid air inlet communication of subcooler, the oxygen-enriched liquid air outlet of lower tower bottom
The oxygen-enriched liquid air inlet communication of cooler；The lean solution Air Export of subcooler passes through 502 pipelines and the poor liquid air inlet communication of upper tower, mistake
By the oxygen-enriched liquid air inlet communication of 503 pipelines and upper tower, the liquid nitrogen outlet of subcooler passes through 501 for the oxygen-enriched liquid air outlet of cooler
Pipeline and the liquid nitrogen inlet communication on upper tower top；The high pure nitrogen outlet of upper top of tower passes through the high-purity of 601 pipelines and subcooler
Nitrogen inlet connects, and the high pure nitrogen outlet of subcooler is high-purity by 504 pipelines and the high pure nitrogen inlet communication of main heat exchanger
High pure nitrogen outlet discharge of the nitrogen through main heat exchanger is collected；The dirty nitrogen outlet on upper tower top is by 602 pipelines with crossing condenser
Dirty nitrogen inlet connection, cross condenser dirty nitrogen outlet is connected by 505 pipelines with the dirty nitrogen inlet of main heat exchanger, dirty nitrogen is through master
The dirty nitrogen outlet discharge of heat exchanger.
According to the device that oxygen rich gas and high pure nitrogen are produced while above-mentioned low energy consumption, the main heat exchanger is aluminum
Plate-fin heat exchanger.
According to the device that oxygen rich gas and high pure nitrogen are produced while above-mentioned low energy consumption, the subcooler is aluminum plate
Fin heat exchanger.
According to the device that oxygen rich gas and high pure nitrogen are produced while above-mentioned low energy consumption, the Shang Ta and lower tower are
Regular packed tower or sieve-plate tower.
The method for producing oxygen rich gas and high pure nitrogen simultaneously using said apparatus, specifically includes following steps：
A, the air from air passes through air compression system successively, and air precooling system and sieve purification system are carried out
Filtering, compression, purification, remove the moisture and carbon dioxide in air, the dry air after being purified, the dry air point
For two-way, enter booster expansion turbine by 101 pipelines all the way, another way enters main heat exchanger by 102 pipelines；
B, into booster expansion turbine dry air be pressurized in booster expansion turbine after, enter by 103 pipelines
Enter in main heat exchanger and cooled down, the expanding end that the dry air after cooling enters booster expansion turbine through 201 pipelines is carried out
Swell refrigeration, the dry air after expansion enter upper tower through 104 pipelines and carry out rectifying separation；
C, the dry air into main heat exchanger is cooled down in main heat exchanger, cooled, the dry air warp after cooling
202 pipelines enter in lower floor main condenser evaporator K2 to be changed as thermal source and the liquid oxygen-enriched in lower floor main condenser evaporator K2
Heat, the dry air after heat exchange enter lower tower through 301 pipelines and carry out preliminary rectifying separation, separated by preliminary rectifying, in Xia Ta
Top obtains high pure nitrogen, and poor liquid air and oxygen-enriched liquid air are obtained in bottom；Wherein, high pure nitrogen enters upper strata master through 401 pipelines
Liquid nitrogen is condensed into condenser/evaporator K1, condensed liquid nitrogen exports row by the liquid nitrogen of upper strata main condenser evaporator K1 bottoms
Go out, two-way is then divided into after 303 pipelines, liquid nitrogen returns in lower tower through 303A pipelines and is used as phegma, another way liquid nitrogen all the way
Enter upper tower through 303B pipelines, subcooler and 501 pipelines and carry out final rectifying separation as phegma；The poor liquid air warp of gained
402 pipelines, subcooler and 502 pipelines enter upper tower and carry out final rectifying separation；The oxygen-enriched liquid air of gained entered through 403 pipelines
Cooled down in cooler, entering upper tower through 503 pipelines after cooling carries out final rectifying separation；
D, separated by the rectifying of upper tower, the high pure nitrogen that upper top of tower obtains, top obtains dirty nitrogen, and bottom obtains liquid
It is oxygen-enriched；Wherein, high pure nitrogen enters in subcooler through 601 pipelines carries out re-heat, enters after re-heat through 504 pipelines in main heat exchanger
Re-heat is carried out, the high pure nitrogen of re-heat to normal temperature is collected by the high pure nitrogen outlet discharge of main heat exchanger, obtains high pure nitrogen production
Product；Dirty nitrogen enters in subcooler through 602 pipelines carries out re-heat, enters after re-heat through 505 pipelines in main heat exchanger and carries out re-heat, multiple
Heat is collected to the dirty nitrogen of normal temperature by the dirty nitrogen outlet discharge of main heat exchanger, obtains dirty nitrogen product；Liquid oxygen-enriched in upper tower is then straight
Tap into the main condenser evaporator K1 of upper strata；Stop valve 1 is opened, closes stop valve 2, liquid oxygen-enriched is in main condenser evaporator K1
It is evaporated, the oxygen rich gas for evaporating gained returns to upper tower participation rectifying as upflowing vapor；Do not have in main condenser evaporator K1
Have through 304 pipelines and stop valve 1 to be entered in lower floor main condenser evaporator K2 by the liquid oxygen-enriched of carburation by evaporation and be vaporized, after vaporization
Obtained oxygen rich gas enters in main heat exchanger through 302 pipelines carries out re-heat, and the oxygen rich gas of re-heat to normal temperature is by main heat exchanger
Oxygen rich gas outlet discharge collect, obtain oxygen rich gas product, for use.
According to above-mentioned method, wherein, in step d, stop valve 1 is being closed, when opening stop valve 2, lower floor's main condenser steams
Hair device K2 does not work, and now device is the conventional cryogenic air separation plant for producing high pure nitrogen and high purity oxygen gas；Pass through
Tower rectifying separation is crossed, obtains high pure nitrogen in upper top of tower, top obtains dirty nitrogen, and bottom obtains liquid high purity oxygen gas, liquid
High purity oxygen gas fully enters in the main condenser evaporator K1 of upper strata and carries out evaporating completely, and the high purity oxygen gas obtained after evaporation is through upper strata master
302 pipelines, which are incorporated to, after condenser/evaporator K1 high purity oxygen gas outlet, 305 pipelines and stop valve 2 carries out re-heat into main heat exchanger,
Re-heat to the high purity oxygen gas of normal temperature is collected by the oxygen rich gas outlet discharge of main heat exchanger, high purity oxygen gas product is obtained, for using.
The positive beneficial effect that the utility model obtains：
(1) the technical solution of the utility model, the dry air after overcompression, precooling, purification are used, fraction enters
Outside pressuring expansion mechanism cold, most of dry air cools down into main heat exchanger.The dry air come out from main heat exchanger is advanced
Enter in lower floor's main condenser evaporator, exchanged heat as thermal source and liquid oxygen-enriched, enter back into Xia Ta bottoms afterwards and participate in rectifying；Meanwhile
The oxygen of liquid oxygen-enriched vaporization does not return to Shang Ta, but directly by being sent out after main heat exchanger rewarming.Due to identical liquefaction temperature
Under degree, compared to nitrogen, the pressure of relatively low air can meet heat transfer requirements, so air compressor in air compression system
Output pressure be minimized to 0.30~0.32MPa, air compressor machine 0.5MPa of more conventional cryogenic air separation unit device or so pressure,
19.6~22.3% energy consumption is reduced, has saved the substantial amounts of energy, there is significant economic benefit and social benefit.
(2) by technical solutions of the utility model, while high pure nitrogen is produced, it can directly produce oxygen purity and exist
The oxygen rich gas of specified purity in the range of 70%-95%, the oxygen rich gas can be used directly for subsequent production, therefore, this reality
Two kinds of products can be produced simultaneously with new technique scheme, are reduced the repeated construction and investment of equipment, are simplified production process,
Reduce production cost.
(3) liquid oxygen-enriched of technical solutions of the utility model main condenser evaporator at the middle and upper levels is cold through stop valve 1 and lower floor master
Solidifying evaporator connection, and oxygen rich gas is not connected with upper tower, upper strata main condenser evaporator caused by lower floor's main condenser evaporator,
But use the structure directly sent out so that lower floor's main condenser evaporator can close as needed, it is achieved thereby that the present apparatus
The adjustment of operating condition；Moreover, when closing stop valve 1, opening stop valve 2, when lower floor main condenser evaporator K2 does not work, this
When device be conventional production high pure nitrogen and high purity oxygen gas cryogenic air separation plant, high pure nitrogen can be produced simultaneously
And high purity oxygen gas, therefore, device of the invention realizes set of device multiple use, reduces the repeated construction and throwing of equipment
Money, reduces production cost.
(4) technical solutions of the utility model, do not change existing high pure nitrogen production technology, do not have to high pure nitrogen production
Influence.
Brief description of the drawings
The structural representation of the device of oxygen rich gas and high pure nitrogen is produced while Fig. 1 the utility model low energy consumption.
In Fig. 1,1 is air compression system, and 2 be air precooling system, and 3 be sieve purification system, and 4 be that turbine boosting is swollen
Swollen machine, 5 be main heat exchanger, and 6 be upper tower, and 7 be lower tower, and 8 be main condenser/evaporator, and 9 be subcooler, and 10 be that valve 1,11 is valve
2。
Embodiment
The utility model is expanded on further below in conjunction with specific embodiment, but is not intended to limit the scope of the utility model.
Embodiment 1：
The device of oxygen rich gas and high pure nitrogen, described device bag are produced referring to Fig. 1, while a kind of low energy consumption of the invention
Include air compression system 1, air precooling system 2, sieve purification system 3, booster expansion turbine 4, main heat exchanger 5, rectifying
Tower and subcooler 9；The air compression system, air precooling system and sieve purification system are the conventional air pressure in this area
Compression system, air precooling system and sieve purification system；The rectifying column includes upper tower 6, lower tower 7 and positioned at Shang Ta, lower tower
Between main condenser evaporator 8, the main condenser evaporator 8 includes upper strata main condenser evaporator K1 and lower floor's main condenser evaporator
Separated between K2, upper strata main condenser evaporator K1 and lower floor main condenser evaporator K2 with dividing plate, upper strata main condenser evaporator K1 with
The upper bottom of tower 6 is spliced and is connected together, and lower floor main condenser evaporator K2 is stitched together with the lower top of tower 7；Between each equipment
It is connected by pipeline, its annexation is：
Air compression system is sequentially communicated with air precooling system, sieve purification system by pipeline, molecular sieve purification
The outlet of system is divided into two-way：
Connected all the way by 101 pipelines with the pressurized end air intlet of booster expansion turbine, booster expansion turbine
Pressurized end air outlet slit passes through 103 pipelines and the pressurized air inlet communication of main heat exchanger, the pressurized air outlet of main heat exchanger
Connected by 201 pipelines with the expanding end air intlet of booster expansion turbine, the expanding end air of booster expansion turbine goes out
Mouth passes through the expanded air inlet communication of 104 pipelines and upper tower；
Another way is connected by 102 pipelines with the air intlet of main heat exchanger, and the air outlet slit of main heat exchanger passes through 202 pipes
Road and lower floor main condenser evaporator K2 air side inlet communication, lower floor main condenser evaporator K2 air side outlet pass through 301
Pipeline and lower tower lower air inlet communication, lower floor main condenser evaporator K2 oxygen rich gas outlet are changed by 302 pipelines and master
The oxygen rich gas inlet communication of hot device, oxygen rich gas outlet discharge of the oxygen rich gas through main heat exchanger are collected；The height on Xia Ta tops
Pure nitrogen gas outlet is connected by 401 pipelines with upper strata main condenser evaporator K1 nitrogen side-entrance, upper strata main condenser evaporator K1
Liquid nitrogen outlet be divided into two-way after 303 pipelines, enter all the way into the liquid nitrogen inlet communication of 303A pipelines and lower tower, another way
The liquid nitrogen inlet communication of 303B pipelines and subcooler, upper strata main condenser evaporator K1 liquid oxygen-enriched outlet by 304 pipelines with
Lower floor main condenser evaporator K2 liquid oxygen-enriched inlet communication, 304 pipelines are provided with valve 1；Upper strata main condenser evaporator K1's
High purity oxygen gas outlet passes through 305 pipelines and 302 pipeline communications, and 305 pipelines are provided with valve 2；The lean solution Air Export of Xia Ta bottoms
By 402 pipelines and the poor liquid air inlet communication of subcooler, the oxygen-enriched liquid air outlet of lower tower bottom passes through 403 pipelines and subcooler
Oxygen-enriched liquid air inlet communication；The lean solution Air Export of subcooler passes through 502 pipelines and the poor liquid air inlet communication of upper tower, subcooler
Oxygen-enriched liquid air outlet by the oxygen-enriched liquid air inlet communication of 503 pipelines and upper tower, the liquid nitrogen outlet of subcooler passes through 501 pipelines
With the liquid nitrogen inlet communication on upper tower top；The high pure nitrogen outlet of upper top of tower passes through 601 pipelines and the high pure nitrogen of subcooler
Inlet communication, the high pure nitrogen outlet of subcooler pass through 504 pipelines and the high pure nitrogen inlet communication of main heat exchanger, high pure nitrogen
High pure nitrogen outlet discharge through main heat exchanger is collected；The dirty nitrogen outlet on upper tower top passes through 602 pipelines and the dirt for crossing condenser
Nitrogen inlet is connected, and the dirty nitrogen outlet for crossing condenser is connected by 505 pipelines with the dirty nitrogen inlet of main heat exchanger, and dirty nitrogen is through main heat exchange
The dirty nitrogen outlet discharge of device is collected.
Wherein, the main heat exchanger and subcooler are aluminum plate-fin heat exchanger；The Shang Ta and lower tower are regular
Packed tower；The valve 1 and valve 2 are stop valve.
Embodiment 2：
Referring to Fig. 1, the content and embodiment 1 of embodiment 2 are essentially the same, and its difference is, the Shang Ta and lower tower
It is sieve-plate tower.
Claims (4)
1. produce the device of oxygen rich gas and high pure nitrogen while a kind of low energy consumption, described device include air compression system,
Air precooling system, sieve purification system, it is characterised in that described device also include booster expansion turbine, main heat exchanger,
Rectifying column and subcooler；The rectifying column includes Shang Ta, lower tower and the main condenser evaporator between Shang Ta, lower tower, described
Main condenser evaporator includes upper strata main condenser evaporator K1 and lower floor main condenser evaporator K2, upper strata main condenser evaporator K1 with
Being separated between layer main condenser evaporator K2 with dividing plate, upper strata main condenser evaporator K1 splices and is connected together with upper tower bottom,
Lower floor main condenser evaporator K2 is stitched together with lower top of tower；It is connected between each equipment by pipeline, its annexation is：
Air compression system is sequentially communicated with air precooling system, sieve purification system by pipeline, sieve purification system
Outlet be divided into two-way：
Connected all the way by 101 pipelines with the pressurized end air intlet of booster expansion turbine, the supercharging of booster expansion turbine
End air outlet slit is passed through by 103 pipelines and the pressurized air inlet communication of main heat exchanger, the pressurized air outlet of main heat exchanger
201 pipelines connect with the expanding end air intlet of booster expansion turbine, and the expanding end air outlet slit of booster expansion turbine leads to
Cross the expanded air inlet communication of 104 pipelines and upper tower；
Another way is connected by 102 pipelines with the air intlet of main heat exchanger, the air outlet slit of main heat exchanger by 202 pipelines with
Lower floor main condenser evaporator K2 air side inlet communication, lower floor main condenser evaporator K2 air side outlet pass through 301 pipelines
With lower tower lower air inlet communication, lower floor main condenser evaporator K2 oxygen rich gas outlet passes through 302 pipelines and main heat exchanger
Oxygen rich gas inlet communication, oxygen rich gas through main heat exchanger oxygen rich gas outlet discharge collect；The High Purity Nitrogen on Xia Ta tops
Gas outlet is connected by 401 pipelines with upper strata main condenser evaporator K1 nitrogen side-entrance, upper strata main condenser evaporator K1 liquid
Nitrogen outlet is divided into two-way after 303 pipelines, enters 303B into 303A pipelines and the liquid nitrogen inlet communication of lower tower, another way all the way
The liquid nitrogen inlet communication of pipeline and subcooler, upper strata main condenser evaporator K1 liquid oxygen-enriched outlet pass through 304 pipelines and lower floor
Main condenser evaporator K2 liquid oxygen-enriched inlet communication, 304 pipelines are provided with valve 1；Upper strata main condenser evaporator K1's is high-purity
Oxygen outlet is provided with valve 2 by 305 pipelines and 302 pipeline communications, 305 pipelines；The lean solution Air Export of Xia Ta bottoms passes through
The poor liquid air inlet communication of 402 pipelines and subcooler, the oxygen-enriched liquid air outlet of lower tower bottom pass through the richness of 403 pipelines and subcooler
Oxygen liquid air inlet communication；The lean solution Air Export of subcooler passes through 502 pipelines and the poor liquid air inlet communication of upper tower, the richness of subcooler
The outlet of oxygen liquid air by the oxygen-enriched liquid air inlet communication of 503 pipelines and upper tower, the liquid nitrogen outlet of subcooler by 501 pipelines with it is upper
The liquid nitrogen inlet communication on tower top；The high pure nitrogen import that the high pure nitrogen outlet of upper top of tower passes through 601 pipelines and subcooler
Connection, the high pure nitrogen outlet of subcooler is by 504 pipelines and the high pure nitrogen inlet communication of main heat exchanger, and high pure nitrogen is through master
The high pure nitrogen outlet discharge of heat exchanger is collected；The dirty nitrogen outlet on upper tower top is entered by 602 pipelines with crossing the dirty nitrogen of condenser
Mouth connection, the dirty nitrogen outlet for crossing condenser are connected by 505 pipelines with the dirty nitrogen inlet of main heat exchanger, and dirty nitrogen is through main heat exchanger
Dirty nitrogen outlet discharge is collected.
2. the device of oxygen rich gas and high pure nitrogen is produced while low energy consumption according to claim 1, it is characterised in that
The main heat exchanger and subcooler are aluminum plate-fin heat exchanger.
3. the device of oxygen rich gas and high pure nitrogen is produced while low energy consumption according to claim 1, it is characterised in that
The Shang Ta and lower tower are regular packed tower or sieve-plate tower.
4. the device of oxygen rich gas and high pure nitrogen is produced while low energy consumption according to claim 1, it is characterised in that
The valve 1 and valve 2 are stop valve.
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| CN201720441525.8U CN206724574U (en) | 2017-04-25 | 2017-04-25 | The device of oxygen rich gas and high pure nitrogen is produced while a kind of low energy consumption |
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| CN201720441525.8U CN206724574U (en) | 2017-04-25 | 2017-04-25 | The device of oxygen rich gas and high pure nitrogen is produced while a kind of low energy consumption |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106989567A (en) * | 2017-04-25 | 2017-07-28 | 河南开元空分集团有限公司 | A kind of apparatus and method that oxygen rich gas and high pure nitrogen are produced while low energy consumption |
| CN108036584A (en) * | 2017-12-28 | 2018-05-15 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification |
| CN108120226A (en) * | 2017-12-28 | 2018-06-05 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen and oxygen is produced from air by cryogenic rectification |
-
2017
- 2017-04-25 CN CN201720441525.8U patent/CN206724574U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106989567A (en) * | 2017-04-25 | 2017-07-28 | 河南开元空分集团有限公司 | A kind of apparatus and method that oxygen rich gas and high pure nitrogen are produced while low energy consumption |
| CN108036584A (en) * | 2017-12-28 | 2018-05-15 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification |
| CN108120226A (en) * | 2017-12-28 | 2018-06-05 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen and oxygen is produced from air by cryogenic rectification |
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