CN106839652A - Health care gas integrated form preparation method and its produce and feedway - Google Patents
Health care gas integrated form preparation method and its produce and feedway Download PDFInfo
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- CN106839652A CN106839652A CN201611178586.6A CN201611178586A CN106839652A CN 106839652 A CN106839652 A CN 106839652A CN 201611178586 A CN201611178586 A CN 201611178586A CN 106839652 A CN106839652 A CN 106839652A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
- 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
- F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
- F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Abstract
The present invention relates to Deep Cooling Method oxygen producing technical field, disclose health care gas integrated form preparation method and its produce and feedway.Including hot junction system, cold end system and back-up system, hot junction system is used for filtering, cooling, the dry purifying of air, gas after the treatment of hot junction is divided into four strands and enters cold end system and back-up system, cold end system includes high-pressure tower and lower pressure column, the liquid oxygen that lower pressure column is produced essentially from high-pressure tower the liquid air rich in oxygen, so as to be obtained reach the pure oxygen of medical standard.By setting oxygen surge tank in technological process, and its operating pressure is improved, when device steady and continuous is operated in metered flow, can just meet the demand of hospital's day and night difference gas consumption.And the present apparatus can simultaneously obtain liquid oxygen, liquid nitrogen, oxygen, nitrogen, medical dry air, in the case where device stops, liquid oxygen storage tank and liquid nitrogen storage are able to maintain that the operation of aspirating pipeline, and present apparatus energy saving, simple to operate, control stabilization.
Description
Technical field
The invention belongs to Deep Cooling Method oxygen producing technical field, more particularly to health care gas integrated form preparation method
And its produce and feedway.
Background technology
Deep Cooling Method is first, by water and titanium dioxide and hydrocarbon substance in air compression, cooling, purification absorption air etc., to change
Exchange heat and make air liquefaction with cold flow stock in hot device, using oxygen, the difference of the boiling point of nitrogen component, oxygen, nitrogen are realized in rectifying column
Separate, here it is air rectification method.
Extensive oxygen processed industrial at present generally uses Deep Cooling Method, the liquid oxygen produced by large-scale cryogenic system, by tank car
It is transported in the low-temperature pressure storage tank in hospital, is used for hospital after being vaporized through air vaporizer, it has the disadvantage liquid
During body supply initiative rests in supplier's hand, there is quality risk, liquid oxygen source is far away, and transport is inconvenient, cost compared with
Height, production liquid oxygen unit energy consumption is higher in addition, and the equivalent price of oxygen is about 3 yuan/Nm3.
Small-sized cryogenic system is only limitted to fill oxygen cylinder and is directly produced liquid oxygen in medical field at present, not a pin
The small-sized cryogenic system for the continuous supply in hospital scene specially designed with gas demand and feature large hospital.And device
Occupation of land is larger, and system of unit oxygen energy consumption is higher, about 1.3~1.5kWh/Nm3.
The compromise method of another kind is to install to be directly produced using pressure-variable adsorption legal system oxygen (i.e. PSA oxygen) device in hospital
Oxygen supply hospital uses, and its general principle is that had selective absorption to the oxygen in air, nitrogen component and made based on molecular sieve
Oxygen nitrogen separation is so as to obtain oxygen in air.When air is through overcompression, through adsorption tower molecular sieve adsorption layer when, nitrogen molecular is excellent
First it is adsorbed, oxygen molecule is stayed turns into product oxygen through adsorption bed in the gas phase.When the nitrogen adsorption in adsorbent layer reaches
When relative saturation, the nitrogen molecular of sorbent molecule adsorption is desorbed and sent out using the method for depressurizing or vacuumizing
Battery limit (BL) is emptied, and adsorbent is obtained desorbing and is recovered original adsorption capacity again, is that the absorption in next cycle is produced oxygen and prepared, two
Adsorption tower is ceaselessly circulated (to contain two) above, is achieved that the continuous purpose for producing oxygen.The oxygen purity that the method is produced leads to
Often there was only 93% or so.Even if taking extreme method, its oxygen purity only up to reach 95%, it is impossible to reach medical oxygen
99.5% purity requirement, so be only suitable for the less demanding occasion of oxygen purity, and Unit consumption for oxygen production is higher, about 1.5~
1.8kWh/Nm3.And cannot simultaneously supply other medical gases, such as nitrogen, drying compressed air, liquid oxygen, liquid nitrogen etc..
The content of the invention
The present invention is technology application extension of the cryogenics in medical treatment ＆ health field, for large hospital to medical gas
Demand and (oxygen consuming amount between 15Nm3/h and 200Nm3/h, day and night gas consumption difference is big, uses oxygen pressure with gas situation
It is 4BarA, in addition it is also necessary to drying compressed air, nitrogen, liquid oxygen, liquid nitrogen), there is provided a kind of health care gas integrated form preparation side
Method and its produce and feedway.
In order to solve above-mentioned technical problem, the present invention is addressed by following technical proposals：
The integrated form preparation method of medical gas, forming steps are as follows：
A. will be again dried after air filtration compression cooling；
B. by dried gas by purifying removal air in harmful constituent such as vapor, CO2, N2O and other dive
Harmful hydrocarbon；
C. the air after dry decontamination in step b is divided into four strands, first burst of air entrance is sent to high-pressure tower after cooling
Used as gas is risen, second strand of air enters lower pressure column rectifying, enters after the 3rd burst of pressurized cooling of air through cooling expansion step-down
High-pressure tower rectifying；4th strand of air enters as dry air to be collected；
D. the air for entering in high-pressure tower in step c obtains nitrogen by rectifying at the top of high-pressure tower, is obtained in bottom
Liquid air rich in oxygen, the liquid air rich in oxygen participates in rectifying by entering lower pressure column after supercooling, and lower pressure column is on top
Portion obtains nitrogen, and the liquid oxygen that the liquid air rich in oxygen from high-pressure tower is obtained by rectifying again is obtained in bottom；
E. a liquid oxygen part for low pressure tower bottom is stored in liquid form, another part liquid oxygen by re-heat, re-heat it is same
First strand, second strand, the 3rd strand of air in Shi Lengning pressure increase steps c, oxygen is stored in a gaseous form after re-heat；Lower pressure column is obtained
The dirty nitrogen for arriving as molecular sieve system dirty nitrogen；A nitrogen part in high-pressure tower is collected through re-heat in the form of nitrogen,
Remaining part is condensed to collect in liquid form；The liquid nitrogen of collection is divided into three parts, a part of backflow as lower pressure column
Liquid nitrogen, a part of backflow liquid nitrogen as high-pressure tower, remaining part stores as liquid nitrogen product.
Preferably, first strand of pressure of air is 5~9BarA, second strand of air is through the pressure after expanded step-down
1.4~1.6BarA, the pressure after the 3rd burst of air pressurized is 15~25BarA, and the operating pressure of high-pressure tower is 5~6BarA, low
The operating pressure for pressing tower is 1.3~1.6BarA.
Preferably, first strand of air is through temperature -165~-175 DEG C after heat exchange, second strand of air is through the temperature after heat exchange
It is -95~-105 DEG C to spend, and the 3rd strand of air is -160~-170 DEG C through the temperature after heat exchange.
A kind of integrated form preparation method for foregoing medical gas produces feeder, including hot junction system, cold end
System and back-up system, hot junction system include air cleaner, air compressor, refrigerator, steam knockout drum, molecular sieve system
And controller, air is successively through air cleaner, air compressor, refrigerator, the filtering of steam knockout drum, pressurization, cooling, drying
The pernicious gas entered afterwards in molecular sieve system removal air, such as vapor, CO2、N2O and other potential harmful nytrons
Thing, the air after being processed through molecular sieve system enters cold end system and back-up system, and the action of molecular sieve system is entered by controller
Row control.
Preferably, hot junction system also include air booster, cold end system include main heat exchanger, subcooler, high-pressure tower,
Compression pump and gas expander in main condenser evaporator, lower pressure column, liquid oxygen, four are divided into by the gas after molecular sieve system treatment
Stock, first burst of remaining part is connected to high-pressure tower after being cooled down through heat exchanger, second strand of air exchanges heat by main heat exchanger, gas
Lower pressure column is connected to after expanding machine step-down cooling, the 3rd strand of air is connected by pipeline after being pressurizeed through air booster through main heat exchanger
High-pressure tower is connected to, the 4th strand enters back-up system as drying compressed air, and main condenser evaporator is arranged on high-pressure tower and low pressure
Between tower, the liquid air rich in oxygen of high pressure tower bottom is connected to lower pressure column by subcooler carries out rectifying again, high-pressure tower
A part for the nitrogen at top is connected to main condenser evaporator condensation into liquid nitrogen by pipeline, and another part nitrogen is through main heat exchanger
8 re-heats enter back-up system, and compression pump is exported with the liquid oxygen of low pressure tower bottom and main heat exchanger is connected in liquid oxygen, and liquid oxygen is by liquid
Oxygen pump boosting enters back-up system.
Preferably, a part for the liquid nitrogen collected through main condenser evaporator is connected to low pressure cooling tower by subcooler making
It is backflow liquid nitrogen, liquid nitrogen another part enters high-pressure tower as backflow liquid nitrogen, and remaining part enters as liquid nitrogen product
Back-up system.
Used as present invention further optimization, back-up system includes liquid oxygen storage tank, liquid nitrogen storage, oxygen surge tank, vaporization
Device, oxygen cylinder charging device and pipe network of supplying gas, the liquid oxygen part that lower pressure column is collected are connected to liquid oxygen internal pressure by liquid oxygen line
Contracting pump, is collected after compression pump in liquid oxygen boosts by liquid oxygen storage tank, and another part liquid oxygen is sent to main heat exchanger, through main heat exchange
After device re-heat, feeding is collected by oxygen surge tank and is supplied gas pipe network, oxygen cylinder charging device is connected to liquid oxygen storage tank, liquid oxygen storage tank warp
Heat exchanger is connected to oxygen surge tank, and liquid nitrogen is collected through subcooler by liquid nitrogen storage, and the path into the nitrogen of back-up system is
Nitrogen outlet from the top of high-pressure tower enters main heat exchanger re-heat, and the nitrogen after re-heat is supplied gas pipe network.
Preferably, molecular sieve system includes heater and at least two molecular sieve adsorbers, heater is used for heating point
Son sieve adsorber regeneration gas, in absorption, one in regeneration for molecular sieve adsorber at least one.
Preferably, heater is electric heater, individual molecule sieve absorber adsorption cycle is 4~8 hours.
Preferably, air compressor is oilless air compressor, the type of cooling is air-cooled, and air booster is oil-free
Formula air booster.Hot junction system is arranged in the container of hot junction, and cold end system is arranged in cold end container.
Using above technological means, the invention has the advantages that：
The present invention can be in hospital scene oxygen producing simultaneously using Deep Cooling Method, nitrogen, liquid oxygen, liquid nitrogen and to dry compression empty
Gas, oxygen purity meets the requirement of medical oxygen 99.5%.Hospital dries compression gas suppling device without being separately configured again.Technique
By setting oxygen surge tank in flow, and its operating pressure is improved, when device steady and continuous is operated in metered flow, with regard to energy
Meet the demand of hospital's day and night difference gas consumption, it is simple to operate, be conducive to the stabilization of device.By setting in technological process
Air booster re-heat liquid oxygen is put, compression in whole liquid oxygen is realized, (oxygen is produced in the small-sized cryogenic system of these oxygen scales processed
Within amount 200Nm3/h) belong to innovation.Air inlet amount is reduced simultaneously, energy consumption is reduced, Unit consumption for oxygen production about 0.8~
0.9kWh/Nm3, and the use of oxygen compressor is avoided, security is improve, can simultaneously meet hospital of hospital public ward end
End, anesthetic, lung ventilator, hyperbaric oxygen chamber is required with oxygen.In the case where device stops, liquid oxygen oxygen in liquid oxygen storage tank can be with
As being promptly fed to aspirating pipeline with gas.And apparatus structure that the present invention is used is compact, floor space is small, installs simple.
Brief description of the drawings
Fig. 1 is the equipment workflow diagram of the embodiment of the present invention.
The toponym that each number designation is referred in accompanying drawing is as follows：1-air cleaner, 2 one air compressors, 3 one
Refrigerator, 4 one steam knockout drums, 5 one molecular sieve adsorbers, 6-electric heater, 7-air booster, 8 one main heat exchangers,
Compression pump, 14-the in 9-gas expander, 10 1 high-pressure towers, 11-lower pressure column, 12-main condenser evaporator, 13-liquid oxygen
One subcooler, the 15-the second subcooler, 16 1 liquid oxygen storage tanks, the 17 one the first air vaporizers, 18 1 liquid oxygen high-pressure piston pumps,
19 one the second air vaporizers, 20 1 oxygen cylinder charging devices, 21 1 liquid nitrogen storages, 22 1 oxygen surge tanks, 23 1 controls
Device.
Specific embodiment
The present invention is described in further detail with embodiment below in conjunction with the accompanying drawings.
The integrated form preparation method of medical gas, forming steps are as follows：
A. will be again dried after air filtration compression cooling；
B. by dried gas by the harmful constituent such as vapor, CO in purifying removal air2、N2O is potential with other
Harmful hydrocarbon；
C. the air after dry decontamination in step b is divided into four strands, first burst of air entrance is sent to high-pressure tower after cooling
10 used as gas is risen, and second strand of air enters the rectifying of lower pressure column 11, enter after the 3rd burst of pressurized cooling of air through cooling step-down
The rectifying of high-pressure tower 10；4th strand of air enters as dry air to be collected；
D. the air for entering in high-pressure tower 10 in step c obtains nitrogen by rectifying at the top of high-pressure tower 10, in bottom
The liquid air rich in oxygen is obtained, the liquid air rich in oxygen participates in rectifying, low pressure by entering lower pressure column 11 after supercooling
Tower 11 obtains nitrogen at top, obtains what the liquid air rich in oxygen from high-pressure tower 10 was obtained by rectifying again in bottom
Liquid oxygen；
E. the bottom of lower pressure column 11 liquid oxygen a part stores in liquid form, another part liquid oxygen by re-heat, re-heat
First strand, second strand, the 3rd strand of air in pressure increase step c are condensed simultaneously, and oxygen is stored in a gaseous form after re-heat；Lower pressure column
The 11 dirty nitrogen for obtaining as molecular sieve system dirty nitrogen；A nitrogen part in high-pressure tower 10 is through re-heat in the form of nitrogen
Collect, remaining part is condensed to collect in liquid form；The liquid nitrogen of collection is divided into three parts, and a part is used as lower pressure column 11
Backflow liquid nitrogen, a part as high-pressure tower 10 backflow liquid nitrogen, remaining part as liquid nitrogen product store.
For large hospital is to the demand of medical gas and uses gas situation, the average oxygen consuming amount of such as hospital is in 50~80Nm3/
H, oxygen pressure is 4BarA, in addition it is also necessary to drying compressed air 200Nm3/ h, 0~5Nm of nitrogen3/ h, 0~2Nm of liquid oxygen3/ h, liquid nitrogen 0
~2Nm3/h。
As shown in figure 1, the integrated form of medical gas is produced and feedway, including hot junction system, cold end system and standby
System, hot junction system includes air cleaner 1, air compressor 2, refrigerator 3, steam knockout drum 4, molecular sieve system and control
Device 23, air filters through air cleaner 1, air compressor 2, refrigerator 3, steam knockout drum 4, pressurizes, cools down, drying successively
Vapor, the CO entered afterwards in molecular sieve system removal air2、N2O, the air after being processed through molecular sieve system, through molecular sieve system
Air after system treatment enters cold end system and back-up system, and the action of molecular sieve system is controlled by controller 23.Hot junction
System also includes air booster 7, and cold end system includes main heat exchanger 8, subcooler, high-pressure tower 10, main condenser evaporator 12, low
Compression pump 13 and gas expander 9 in pressure tower 11, liquid oxygen, four strands, first strand are divided into by the gas after molecular sieve system treatment
Remaining part is connected to high-pressure tower 10 after being cooled down through heat exchanger, and second strand of air exchanges heat by main heat exchanger 8, gas expander
Lower pressure column 11 is connected to after 9 step-down coolings, the 3rd strand of air is connected by pipeline after being pressurizeed through air booster 7 through main heat exchanger 8
High-pressure tower 10 is connected to, the 4th strand enters back-up system as drying compressed air, and main condenser evaporator 12 is arranged on high-pressure tower 10
And lower pressure column 11 between, the liquid air rich in oxygen of the bottom of high-pressure tower 10 is connected to lower pressure column 11 by subcooler to be carried out again
Rectifying a, part for the nitrogen at the top of high-pressure tower 10 is connected to main condenser evaporator 12 and is condensed into liquid nitrogen, another portion by pipeline
Nitrogen is divided to enter back-up system through the re-heat of main heat exchanger 8, compression pump 13 and the liquid oxygen outlet of the bottom of lower pressure column 11 and master in liquid oxygen
Heat exchanger 8 is connected, and liquid oxygen enters back-up system by liquid oxygen pump boosting.A part for the liquid nitrogen collected through main condenser evaporator 12
Lower pressure column 11 is connected to as backflow liquid nitrogen by subcooler, and liquid nitrogen another part enters high-pressure tower 10 as backflow liquid nitrogen, remains
Under part enter back-up system as liquid nitrogen product.Back-up system includes that liquid oxygen storage tank 16, liquid nitrogen storage 21, oxygen delay
Tank 22, vaporizer, oxygen cylinder charging device 20 and pipe network of supplying gas are rushed, the liquid oxygen part that lower pressure column 11 is collected passes through liquid oxygen line
Compression pump 13 in liquid oxygen are connected to, are collected by liquid oxygen storage tank 16 after compression pump in liquid oxygen 13 boosts, another part liquid oxygen quilt
Be sent to main heat exchanger 8, through the re-heat of main heat exchanger 8 after, feeding is collected by oxygen surge tank 22 and is supplied gas pipe network, oxygen cylinder charging device
20 are connected to liquid oxygen storage tank 16, and liquid oxygen storage tank 16 is connected to oxygen surge tank 22 through heat exchanger, and liquid nitrogen is store through subcooler by liquid nitrogen
Groove 21 is collected, and is that nitrogen outlet from the top of high-pressure tower 10 enters the re-heat of main heat exchanger 8 into the path of the nitrogen of back-up system,
Nitrogen after re-heat is supplied gas pipe network.
Molecular sieve system includes heater and at least two molecular sieve adsorbers 5, and heater is used to heat molecular sieve adsorption
The regeneration gas of device 5, in absorption, one is regenerating molecular sieve adsorber 5 at least one, and heater is electric heater 6, individual molecule
Sieve absorber 5 adsorption cycle is 4~8 hours.
Device ice chest if it need to install indoors is highly no more than 5m, and noise is less than 70dB.
Device workflow is as follows：
500~the 650Nm of air of suction3/ h is miscellaneous to remove dust and other milli machines by air cleaner 1 first
Matter, is then compressed to 5.5~9.5BarA through an air compressor 2.
Compressed air is cooled down into refrigerator 3, and moisture is separated in steam knockout drum 4, and compressed air goes out steam knockout drum 4
About 5~10 DEG C of temperature.
Dried compressed air into molecular sieve system purify, in air retain harmful constituent such as vapor,
CO2、N2A suction in two molecular sieve adsorbers 5 that O and other potential harmful hydrocarbons pass through regeneration alternate with each other
It is attached.When one molecular sieve adsorber 5 is adsorbed, another molecular sieve adsorber 5 regenerates.Monotubular adsorption cycle about 4~8 hours.
Wherein dirty nitrogen of the regeneration gas of molecular sieve system from the output of distillation system mesolow tower 11, from lower pressure column 11
Dirty nitrogen 150~170 DEG C are heated in electric heater 6.Molecular sieve is arrived in cold blowing stage dirt nitrogen bypass electric heater 6
Heat is blown down in absorber 5.After regeneration cycle terminates, the molecular sieve adsorber 5 after regeneration is started working, while another
Molecular sieve adsorber 5 proceeds by new regeneration cycle.
The circulation of molecular sieve system automatically controls completion by controller 23 (DCS or PLC).
The processing air of dry decontamination is divided into four strands for about 20 DEG C by temperature after molecular sieve adsorption unit, and first burst of compression is empty
Gas is close to air liquefaction temperature and is then fed into high-pressure tower 10 into the cooling of main heat exchanger 8.Second is extracted in heat exchanger stage casing
Stock compressed air is about 50~100Nm3/ h expands to gas expander 9, and compressed air inlet pressure is about 5.3~9.3BarA,
About -95~-105 DEG C of inlet temperature, this burst of air pressure is about 1.4~1.6BarA and is fed to the conduct of lower pressure column 11 after expansion
Rise gas.3rd burst of compressed air is about 100~150Nm3/h air inlets supercharger 7 and is further compressed to 15~25BarA,
It is then fed into main heat exchanger 8 exchanging heat, the compressed air of heat exchanger hypomere has liquefied, and is all decompressed to about through choke valve
Enter the bottom of high-pressure tower 10 after 6BarA.4th strand of compressed air pressure reduces to one after being about 5~9BarA extractions by pressure-reducing valve
After constant-pressure pipe network is sent as drying compressed air..Wherein first strand air through main heat exchanger 8 exchange heat after temperature -165~-
175 DEG C, the temperature after second strand of air exchanges heat through main heat exchanger 8 is -95~-105 DEG C, and the 3rd strand of air is changed through main heat exchanger 8
Temperature after heat is -160~-170 DEG C.
Air obtains pure nitrogen gas and is obtained rich in oxygen in tower bottom by rectifying at the top of tower in high-pressure tower 10
Liquid air, obtains the liquid air rich in oxygen and carries out rectifying again into lower pressure column 11 by the second subcooler 15 obtaining product
Liquid oxygen.The operating pressure of high-pressure tower is 5~6BarA, and the operating pressure of lower pressure column is 1.3~1.6BarA.
Backflow liquid nitrogen needed for high-pressure tower 10 and the rectifying of lower pressure column 11 comes from main condenser evaporator 12, from high-pressure tower 10
Nitrogen is liquefied as liquid into the main condenser evaporator 12 of the bottom of lower pressure column 11 by nitrogen pipeline by the liquid oxygen of the bottom of lower pressure column 11
Nitrogen.Liquid nitrogen after being liquefied is divided into the phegma that three strands of one liquid nitrogen are used as high-pressure tower 10, and one liquid nitrogen is in the first mistake
Deutomerite is subcooled in cooler 14 and streams to the top of lower pressure column 11 as phegma, remaining part is extracted as liquid nitrogen product and is stored in
Liquid nitrogen storage 21, the amount of liquid nitrogen product is 0~3Nm3/h.Liquid nitrogen storage 21 is connected to the top of lower pressure column 11 by pipeline, when
When gas expander 9 is stopped, the liquid nitrogen in liquid nitrogen storage 21 can be back to lower pressure column 11 so as to holding meanss cold balancing,
Continue continuous operation.When liquid nitrogen storage 21 is fitted without, and gas expander 9 is when being stopped, in liquid oxygen storage tank 16
Liquid oxygen is connected by pipeline counter can be noted into main heat exchanger 8 so as to ensure cooling for the 3rd strand of air, holding meanss cold
Balance, continues to device and continuously runs.
In 0~5Nm of gas nitrogen that the tip position of high-pressure tower 10 is extracted3/ h is sent to the re-heat of main heat exchanger 8 to close to atmospheric temperature
After go out main heat exchanger 8 feeding aspirating pipeline.
The liquid air rich in oxygen from the bottom of high-pressure tower 10, participates in exchanging heat by the second subcooler 15, finally send
Rectifying is participated in lower pressure column 11, so as to be obtained in bottom in the isolated pure nitrogen gas of top of tower by rectifying in lower pressure column 11
Pure oxygen, due to the relatively low use demand for being unsatisfactory for hospital of the nitrogen pressure in lower pressure column 11, so from less than the tower top of lower pressure column 11
One section extract dirty nitrogen and send into molecular sieve system after the first subcooler 14, the second subcooler 15 and the re-heat of main heat exchanger 8, make
It is the regeneration gas of molecular sieve system.
Liquid oxygen product is extracted in the bottom position of lower pressure column 11.A part of 50~80Nm of liquid oxygen3/ h delivers to liquid oxygen pump and is pressurized to 7
~11BarA, after the pressure needed for being pressurized to through pump, a part of liquid oxygen delivers to liquid oxygen storage tank 16 after supercooling, and another part is sent to
Main heat exchanger 8 re-heat, there liquid oxygen evaporation condenses pressurized air, and the oxygen after vaporization continues re-heat in main heat exchanger 8
Extremely go out main heat exchanger 8 close to after atmospheric temperature, and deliver to the about 30m of oxygen surge tank 223, make its operating pressure maintain 6~
Between 10BarA, between be decompressed to about 4BarA by pressure-reducing valve and deliver to the oxygen pipe network of hospital, or deliver to bus-bar and carry out oxygen
Bottle is filled.Wherein 16 point of three tunnel of liquid oxygen storage tank respectively connected oxygen pipe network, oxygen cylinder charging device 20, oxygen surge tank 22.
The first air vaporizer 17 is provided between liquid oxygen storage tank 16 and oxygen pipe network；Liquid oxygen storage tank 16 and oxygen cylinder charging device 20 it
Between be provided with the air vaporizer 19 of liquid oxygen high-pressure piston pump 18 and second；Once device stops, the liquid oxygen of the storage of liquid oxygen storage tank 16
Can be used to ensure that oxygen supply.From 5m350~80Nm3/h of liquid oxygen that vacuum pressure storage tank is extracted out, through the first air vaporizer
17 evaporations, into oxygen pipe network.
Wherein air compressor 2 is oilless air compressor, and the type of cooling is air-cooled；Air booster 7 is oil free type
Piston pressurizers；Flow air is cooled to condensing temperature by main heat exchanger 8 for plate sticks up formula heat exchanger, while heating product gas；
First subcooler 14 and the second subcooler 15 use plate type heat exchanger；Compression pump 13 and gas expander 9 are equal wherein in liquid oxygen
It is the using and the reserved, so as to improve the security and operational reliability of device；Main condenser evaporator 12 is designed using bath.
The integrated form of medical gas produces the integrated form preparation method that medical gas is applied to feedway.
In a word, presently preferred embodiments of the present invention, all equalizations made according to scope of the present invention patent be the foregoing is only
Change and modification, should all belong to the covering scope of patent of the present invention.
Claims (10)
1. the integrated form preparation method of medical gas, it is characterised in that：Forming steps are as follows：
A. will be again dried after air filtration compression cooling；
B. dried gas is further removed into vapor, CO by purifying2、N2O；
C. the air after dry decontamination in step b is divided into four strands, first burst of air entrance is sent to high-pressure tower (10) after cooling
Used as gas is risen, second strand of air enters lower pressure column (11) rectifying after cooling step-down, and the 3rd burst of pressurized cooling of air is laggard
Enter high-pressure tower (10) rectifying；4th strand of air is collected as dry air；
D. in step c into high-pressure tower (10) first strand of air and the 3rd strand of air by rectifying high-pressure tower (10) top
Nitrogen is obtained, the liquid air rich in oxygen is obtained in bottom, the liquid air rich in oxygen is by entering lower pressure column after supercooling
(11) rectifying is participated in, lower pressure column (11) obtains nitrogen at top, the liquid rich in oxygen from high-pressure tower (10) is obtained in bottom
The liquid oxygen that state air is obtained by rectifying again；
E. the liquid oxygen part of lower pressure column (11) bottom is stored in liquid form, another part liquid oxygen by re-heat, re-heat it is same
First strand, second strand, the 3rd strand of air in Shi Lengning pressure increase steps c, oxygen is stored in a gaseous form after re-heat；Lower pressure column
(11) the dirty nitrogen for obtaining as molecular sieve system dirty nitrogen；A nitrogen part in high-pressure tower (10) is through re-heat with nitrogen
Form is collected, and remaining part is condensed to collect in liquid form；The liquid nitrogen of collection is divided into three parts, and a part is used as low pressure
The backflow liquid nitrogen of tower (11), a part of backflow liquid nitrogen as high-pressure tower (10), remaining part stores as liquid nitrogen product.
2. the integrated form preparation method of medical gas according to claim 1, it is characterised in that：First strand of pressure of air
It is 5~9BarA, the pressure after second burst of expanded step-down of air is 1.4~1.6BarA, the pressure after the 3rd burst of air pressurized
It is 15~25BarA, the operating pressure of high-pressure tower is 5~6BarA, and the operating pressure of lower pressure column is 1.3~1.6BarA.
3. the integrated form preparation method of medical gas according to claim 1, it is characterised in that：First strand of air is through heat exchange
Temperature -165~-175 DEG C afterwards, second strand of air is -95~-105 DEG C through the temperature after heat exchange, and the 3rd strand of air is after heat exchange
Temperature be -160~-170 DEG C.
4. the integrated form preparation method of medical gas according to claim 1, it is characterised in that：Further gone in step b
Harmful hydrocarbon in except air.
5. the integrated form of medical gas is produced and feedway, including hot junction system, cold end system and back-up system, and its feature exists
In：Hot junction system includes air cleaner (1), air compressor (2), refrigerator (3), steam knockout drum (4), molecular sieve system
With controller (23), air is successively through air cleaner (1), air compressor (2), refrigerator (3), steam knockout drum (4) mistake
Filter, pressurization, cooling, dry after enter molecular sieve system removal air in vapor, CO2、N2O, after being processed through molecular sieve system
Air, through molecular sieve system process after air enter cold end system and back-up system, the action of molecular sieve system is by controlling
Device (23) is controlled.
6. the integrated form of medical gas according to claim 5 is produced and feedway, it is characterised in that：Hot junction system is also
Including air booster (7), cold end system include main heat exchanger (8), subcooler, high-pressure tower (10), main condenser evaporator (12),
Compression pump (13) and gas expander (9) in lower pressure column (11), liquid oxygen, four are divided into by the gas after molecular sieve system treatment
Stock, first burst of remaining part is connected to high-pressure tower (10) after being cooled down through heat exchanger, and second strand of air is changed by main heat exchanger (8)
Lower pressure column (11) is connected to after heat, gas expander (9) step-down cooling, the 3rd strand of air leads to after being pressurizeed through air booster (7)
Piping is connected to high-pressure tower (10) through main heat exchanger (8), and the 4th strand enters back-up system, main condenser as drying compressed air
Evaporator (12) is arranged between high-pressure tower (10) and lower pressure column (11), the liquid air rich in oxygen of high-pressure tower (10) bottom
Being connected to lower pressure column (11) by subcooler carries out rectifying again, and a part for the nitrogen at the top of high-pressure tower (10) is connected by pipeline
Liquid nitrogen is condensed into main condenser evaporator (12), another part nitrogen enters back-up system through main heat exchanger (8) re-heat, in liquid oxygen
Compression pump (13) is exported with the liquid oxygen of lower pressure column (11) bottom and main heat exchanger (8) is connected, and liquid oxygen boosts by liquid oxygen pump and enters
Back-up system.
7. the integrated form of medical gas according to claim 6 is produced and feedway, it is characterised in that：Steamed through main condenser
A part for the liquid nitrogen that hair device (12) is collected is connected to lower pressure column (11) as backflow liquid nitrogen, liquid nitrogen another part by subcooler
Into high-pressure tower (10) as backflow liquid nitrogen, remaining part enters back-up system as liquid nitrogen product.
8. the integrated form of medical gas according to claim 7 is produced and feedway, it is characterised in that：Back-up system bag
Include liquid oxygen storage tank (16), liquid nitrogen storage (21), oxygen surge tank (22), vaporizer, oxygen cylinder charging device (20) and snorkel
Net, the liquid oxygen part that lower pressure column (11) is collected is connected to compression pump in liquid oxygen (13) by liquid oxygen line, by liquid oxygen internal pressure
Collected by liquid oxygen storage tank (16) after contracting pump (13) boosting, another part liquid oxygen is sent to main heat exchanger (8), through main heat exchanger (8)
After re-heat, feeding is collected by oxygen surge tank (22) and is supplied gas pipe network, oxygen cylinder charging device (20) is connected to liquid oxygen storage tank (16),
Liquid oxygen storage tank (16) is connected to oxygen surge tank (22) through heat exchanger, and liquid nitrogen is collected through subcooler by liquid nitrogen storage (21), is entered
The path of the nitrogen of back-up system is that the nitrogen outlet from the top of high-pressure tower (10) enters main heat exchanger (8) re-heat, after re-heat
Nitrogen is supplied gas pipe network.
9. the integrated form of medical gas according to claim 5 is produced and feedway, it is characterised in that：Molecular sieve system
Including heater and at least two molecular sieve adsorbers (5), heater is used to heat the regeneration gas of molecular sieve adsorber 5, molecule
, in absorption, one in regeneration for sieve absorber (5) at least one.
10. the integrated form of medical gas according to claim 9 is produced and feedway, it is characterised in that：Heater is
Electric heater (6), individual molecule sieve absorber (5) adsorption cycle is 4~8 hours.
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| WO2019127009A1 (en) * | 2017-12-26 | 2019-07-04 | 乔治洛德方法研究和开发液化空气有限公司 | System and method for supplying backup product in air separation device |
| CN110155962A (en) * | 2019-07-02 | 2019-08-23 | 上海悟道机电设备有限公司 | Small-sized nitrogen inflating machine processed |
| CN111406191A (en) * | 2017-12-25 | 2020-07-10 | 乔治洛德方法研究和开发液化空气有限公司 | Single package air separation plant with reverse main heat exchanger |
| CN112654827A (en) * | 2018-10-09 | 2021-04-13 | 林德有限责任公司 | Method and air separation plant for extracting one or more air products |
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