CN204923686U - Low -purity oxygen air separation's device - Google Patents

Low -purity oxygen air separation's device Download PDF

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Publication number
CN204923686U
CN204923686U CN201520593333.XU CN201520593333U CN204923686U CN 204923686 U CN204923686 U CN 204923686U CN 201520593333 U CN201520593333 U CN 201520593333U CN 204923686 U CN204923686 U CN 204923686U
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China
Prior art keywords
tower
pipeline
pressure
low
high pressure
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CN201520593333.XU
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Chinese (zh)
Inventor
郑三七
王庆波
孙宇
翟彦邦
李美玲
孟松涛
张建松
赵雪莉
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KAIFENG AIR SEPARATION GROUP CO Ltd
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KAIFENG AIR SEPARATION GROUP CO Ltd
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Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04006Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078Providing 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
    • F25J3/0409Providing 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04006Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078Providing 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
    • F25J3/04103Providing 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 using solely hydrostatic liquid head
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04151Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206Division 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04248Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284Generation 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
    • F25J3/0429Generation 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
    • F25J3/04303Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04436Processes 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 at least a triple pressure main column system
    • F25J3/04448Processes 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 at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/20Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00Processes characterised by the type or other details of the product stream
    • F25J2215/50Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00Details related to the use of reboiler-condensers
    • F25J2250/30External 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
    • F25J2250/40One fluid being air
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00Details related to the use of reboiler-condensers
    • F25J2250/30External 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
    • F25J2250/50One fluid being oxygen

Abstract

The utility model relates to a production low -purity oxygen air separation's novel device, the device include air generation system, front end precooling purification system and cold box, air generation system includes low pressure air compressor machine, heavy pressure air compressor machine, the cold box includes the expansion end and the fractionating tower of main heat exchanger, liquid oxygen evaporimeter, expander, the rectifying column include low pressure lower column, heavy pressure lower column, upper column, low pressure lower column condensing evaporator and be located the upper column and the heavy pressure lower column between condensing evaporator. The utility model discloses fully excavated the rectification potentiality of rectifying column, the energy consumption is low, has hanged down more than 10% than conventional double tower flow, it is simpler than pure oxygen and air mixing in the operation, the product extraction percentage is up to more than 99%.

Description

A kind of device of low purity oxygen air separation
Technical field
The utility model relates to air separation field, particularly relates to a kind of device of low purity oxygen air separation.
Background technology
At present, the air-separating plant of deep cooling low temperature process is widely used in the industry such as chemical industry and metallurgy industry, and oxygen purity requirement is high, and oxygen purity needed for the industry such as Coal Chemical Industry, steel-making is more than 99.6%.And in some field, do not need the pure oxygen of more than 99.6%, oxygen enrichment just can meet the demands, oxygen purity is 70% ~ 97%, the oxygen purity required as fields such as nonferrous smelting, oxygen-enriched combusting, generatings is about about 95%, the not high 0.4bar ~ 2bar of oxygen pressure, can meet the drag losses of course of conveying.Oxygen enrichment sky point has very large market, as 200MWe oxygen enrichment fire coal just needs purity 95% oxygen enrichment 123000Nm in reality industry with following 3/ h.
The raw material of air separation unit is air, and its main consumption is the energy, and therefore, how further, reduction energy ezpenditure seems particularly important.For the complete set of equipments adopting cryogenic rectification, recovery rate and energy consumption become the major parameter evaluating complete set of equipments economic indicator and technical indicator; Air separation unit is large electricity consumer, when energy growing tension, for the user without industry different field, for they provide more low energy consumption more reasonably technological process, development and production go out the complexes of low energy consumption, not only can accomplish to reduce energy consumption, reduce production cost, improve overall economic benefit, also can play certain mitigation to the energy demand be becoming tight day.
The minimum separation merit of cryogenic air separation oxygen generating plant is determined by device oxygen making amount and process pressure, and when amount of oxygen is certain, oxygen purity reduces, and the minimum separation merit needed for air separation reduces, and oxygen energy consumption reduces.Therefore, to low-purity oxygen generating plant, making oxygen that can not be still traditional is routinely treated, and should tap the latent power from the aspect such as rectifying, process organization, and research new device, to reduce oxygen power consumption.
The flow process that current low-purity oxygen equipment adopts remains traditional two-tower rectification, or adopts the method for high-purity oxygen mixing air to obtain.Adopt above two kinds of methods to produce for low purity oxygen equipment, energy consumption is high, less economical.
Utility model content
The purpose of this utility model is to overcome above-mentioned deficiency of the prior art and provides that a kind of energy consumption is low, the device of the low purity oxygen air separation of good economy performance.
The technical solution of the utility model is achieved in that a kind of device of low purity oxygen air separation, comprise air compression system, front end precooling purification system and ice chest, described air compression system comprises low-pressure air compressor machine and high pressure air compressor machine, described ice chest comprises main heat exchanger, liquid oxygen evaporator, the expanding end of decompressor and rectifying column, described rectifying column comprises tower under low-pressure, tower under high pressure, upper tower, tower condenser/evaporator and the condenser/evaporator under upper tower and high pressure between tower under low-pressure, described low-pressure air compressor machine is connected with front end precooling purification system by the first pipeline, first gas vent of described front end precooling purification system is connected with tower under described low-pressure through main heat exchanger by second pipe, second gas vent of front end precooling purification system is connected with the pressurized end of a decompressor by the 3rd pipeline, described pressurized end connects a water cooler by the 4th pipeline, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline, 3rd gas vent of described front end precooling purification system is connected with described high pressure air compressor machine by the 6th pipeline, and in high pressure air compressor machine, outlet port is connected with tower under described high pressure through main heat exchanger by the 7th pipeline, the outlet of high pressure air compressor machine final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 8th pipeline, described liquid oxygen evaporator is connected to tower centre entrance place under described high pressure by the 9th pipeline and first throttle valve, and described liquid oxygen evaporator is connected to tower centre entrance place under described low-pressure by the tenth pipeline and second throttle, described expanding end outlet arranges the 11 pipeline and is connected with upper tower, under described high pressure, tower bottom liquid outlet is by being connected with described low-pressure tower condenser after the 12 pipeline and the 3rd choke valve, under described high pressure, tower central liquid exit connects the 13 pipeline, under described high pressure, the liquid outlet of top of tower connects the 14 pipeline, described 13 pipeline is connected to described upper tower centre entrance place after a subcooler and the 4th choke valve, and described 14 pipeline is connected to described upper top of tower porch after described subcooler and the 5th choke valve, under described low-pressure, tower bottom liquid outlet is connected with described low-pressure tower condenser by the 15 pipeline and the 6th choke valve, under described low-pressure, the liquid outlet of top of tower connects the 16 pipeline, described 16 pipeline is connected to the upper entrance place of described upper tower after described subcooler and the 7th choke valve, and under described low-pressure, the dirty nitrogen of tower condenser is connected with upper tower centre entrance by the 17 pipeline, the dirty nitrogen outlet place of described upper top of tower connects the 18 pipeline, and described 18 pipeline connects described subcooler and main heat exchanger, the liquid oxygen side outlet place of described condenser/evaporator is connected with described liquid oxygen evaporator by the 19 pipeline, and the gas oxygen outlet of described liquid oxygen evaporator is connected with described main heat exchanger by the 20 pipeline.
Under described low-pressure, tower is operating pressure 0.2 ~ 0.22MPa, and under described high pressure, tower is operating pressure ~ 0.36MPa.
Under described high pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, under described low-pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, described upper tower to be the number of plates be 30 ~ 40 or corresponding tower tray number be 52 ~ 68 dishes structured packings on tower.
Take out two-part in high pressure air compressor machine band described in described low-pressure air compressor machine pressure at expulsion 0.25 ~ 0.27MPa., in take out pressure 0.38, last stage pressure ~ 0.65MPa, can according to different oxygen pressure operating mode, adjustment last stage pressure.
A method for low purity oxygen air separation, the method is as follows:
Air is divided into three parts through the compression of low-pressure air compressor machine after front end precooling purifying: Part I air enters main heat exchanger, the gas that backflowed cooling laggard enter tower under low-pressure; The air that Part II is equivalent to swell increment enters the pressurized end supercharging of turbo-expander, after supercharging through cooler cooling laggard enter main heat exchanger, extract out in the middle part of main heat exchanger after being cooled to uniform temperature and enter decompressor, the air after expansion sends into upper tower; Part III air enters the compression of high pressure air compressor machine, extract out after a part enters main heat exchanger cooling and enter tower under high pressure, remainder compresses further through high pressure air compressor machine, liquid oxygen evaporator is entered as thermal source liquid oxygen vaporisation after main heat exchanger cooling, be divided into two strands after going out liquid oxygen evaporator: one enters under high pressure in the middle part of tower, another stock to enter under low-pressure in the middle part of tower; Air, after lower tower rectifying, obtains liquid air at lower tower bottom, obtains liquid nitrogen at top;
Wherein, under high pressure, tower produces liquid nitrogen, lean solution sky and oxygen-enriched liquid air from top to bottom, under oxygen-enriched liquid air throttling enters low-pressure, tower condenser is as low-temperature receiver, lean solution empty through subcooler cross cold after, throttling enters Shang Ta, as its phegma, pure liquid nitrogen is crossed top of tower in cold rear feeding and is made phegma in subcooler; Under low-pressure, tower produces liquid nitrogen and oxygen-enriched liquid air from top to bottom, under oxygen-enriched liquid air throttling enters low-pressure, tower condenser is as low-temperature receiver, liquid nitrogen is crossed top of tower in cold rear feeding and is made phegma in subcooler, and the liquid air vapo r under low-pressure after the evaporation of tower condenser is sent in the middle part of upper tower and participated in rectifying; Nitrogen and liquid oxygen is produced from top to bottom at upper tower, nitrogen extract out from upper top of tower after through subcooler and main heat exchanger re-heat to design temperature cooling box, one dirty nitrogen is used for the regeneration of molecular sieve adsorber, another stock is delivered to water-cooling tower and is cooled water, also have sub-fraction to enter ice chest, ice chest is inflated; Liquid oxygen is extracted out from upper tower bottom and is entered liquid oxygen evaporator, is heated by the air that vaporization is laggard to be entered to be sent to user after main heat exchanger re-heat to normal temperature.
The gas of decompressor pressurized end is from the gas after low-pressure air compressor machine.
Product oxygen purity 70% ~ 97%, product oxygen pressure 0.4bar(G) ~ 2bar(G), oxygen extraction ratio more than 99%.
The conventional double-column process of air separation unit observable index is low more than 10%.
The good effect that the technical solution of the utility model produces is as follows: described low-pressure air compressor machine pressure at expulsion 0.25 ~ 0.27MPa, plant energy consumption has had the reduction of matter.Take out two-part in described high pressure air compressor machine band, in take out pressure 0.38, last stage pressure is about 0.65MPa, can according to different oxygen pressure operating mode, adjustment last stage pressure.
Under described low-pressure, tower is operating pressure 0.2 ~ 0.22MPa, and under described high pressure, tower is operating pressure ~ 0.36MPa.
The utility model has fully excavated the rectifying potentiality of rectifying column, and energy consumption is low, lower than conventional double-column process by more than 10%; Operation mix simple than pure oxygen and air; Product recovery rate is up to more than 99%.
The utility model is different from conventional double-column process air separation unit, the utility model has fully excavated the rectifying potentiality of rectifying column, by the rationalization of flow process, three towers (on high pressure Xia Ta, low-pressure Xia Ta, a platform tower) flow process is adopted to produce low purity oxygen, the row pressure of low-pressure air compressor machine has dropped to 0.27MPa from 0.4MPa, and air compressor machine is the large electricity consumer of air separation unit, the reduction of air compressor machine row pressure has made the conventional double-column process of the overall observable index of air separation unit low nearly 10%.This utility model, to reduction production cost, is increased economic efficiency significant.
Accompanying drawing explanation
Fig. 1 is the structural representation that the utility model produces the device and method of low purity oxygen air separation.
Be labeled as in figure: 1, low-pressure air compressor machine; 2, front end precooling purification system; 3, high pressure air compressor machine; 4, pressurized end; 5, water cooler; 6, main heat exchanger; 7, liquid oxygen evaporator; 8, tower under high pressure; 9, condenser/evaporator; 10, Shang Ta; 11, subcooler; 12, tower under low-pressure; 13, tower condenser/evaporator under low-pressure; 14, expanding end; 15, first throttle valve; 16, second throttle; 17, the 3rd choke valve; 18, the 4th choke valve; 19, the 5th choke valve; 20, the 6th choke valve; 21, the 7th choke valve; 22, ice chest; 101, the first pipeline; 102, second pipe; 103, the 3rd pipeline; 104, the 4th pipeline; 105, the 5th pipeline; 106, the 6th pipeline; 107, the 7th pipeline; 108, the 8th pipeline; 109, the 9th pipeline; 110, the tenth pipeline; 111, the 11 pipeline; 112, the 12 pipeline; 113, the 13 pipeline; 114, the 14 pipeline; 115, the 15 pipeline; 116, the 16 pipeline; 117, the 17 pipeline; 118, the 18 pipeline; 119, the 19 pipeline; 120, the 20 pipeline.
Detailed description of the invention
Below in conjunction with specific embodiment, the utility model is further elaborated.
Embodiment one
A kind of device of low purity oxygen air separation, as shown in Figure 1, comprise air compression system, front end precooling purification system 2 and ice chest 22, described air compression system comprises low-pressure air compressor machine 1 and high pressure air compressor machine 3, described ice chest comprises main heat exchanger 6, liquid oxygen evaporator 7, the expanding end 14 of decompressor and rectifying column, and described rectifying column comprises tower condenser/evaporator 13 and the condenser/evaporator under upper tower and high pressure between tower 9 under tower 8 under tower 12 under low-pressure, high pressure, upper tower 10, low-pressure; Described low-pressure air compressor machine is connected with front end precooling purification system by the first pipeline 101, and the first gas vent of described front end precooling purification system is connected with tower under described low-pressure through main heat exchanger by second pipe 102; Second gas vent of front end precooling purification system is connected with the pressurized end 4 of a decompressor by the 3rd pipeline 103, described pressurized end connects a water cooler 11 by the 4th pipeline 104, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline 105; 3rd gas vent of described front end precooling purification system is connected with described high pressure air compressor machine by the 6th pipeline 106, and in high pressure air compressor machine, outlet port is connected with tower under described high pressure through main heat exchanger by the 7th pipeline 107; The outlet of high pressure air compressor machine final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 8th pipeline 108, described liquid oxygen evaporator is connected to tower centre entrance place under described high pressure by the 9th pipeline 109 and first throttle valve 15, and described liquid oxygen evaporator is connected to tower centre entrance place under described low-pressure by the tenth pipeline 110 and second throttle 16; Described expanding end outlet arranges the 11 pipeline 111 and is connected with upper tower; Under described high pressure, tower bottom liquid outlet is by being connected with described low-pressure tower condenser after the 12 pipeline 112 and the 3rd choke valve 17, under described high pressure, tower central liquid exit connects the 13 pipeline 113, under described high pressure, the liquid outlet of top of tower connects the 14 pipeline 114, described 13 pipeline is connected to described upper tower centre entrance place after a subcooler and the 4th choke valve 18, and described 14 pipeline is connected to described upper top of tower porch after described subcooler and the 5th choke valve 19; Under described low-pressure, tower bottom liquid outlet is connected with described low-pressure tower condenser by the 15 pipeline 115, under described low-pressure, the liquid outlet of top of tower connects the 16 pipeline 116, described 16 pipeline is connected to the upper entrance place of described upper tower after described subcooler and the 6th choke valve 20, and under described low-pressure, the dirty nitrogen of tower condenser is connected with upper tower centre entrance by the 17 pipeline 117; The dirty nitrogen outlet place of described upper top of tower connects the 18 pipeline 118, and described 18 pipeline connects described subcooler and main heat exchanger; The liquid oxygen side outlet place of described condenser/evaporator is connected with described liquid oxygen evaporator by the 19 pipeline 119, and the gas oxygen outlet of described liquid oxygen evaporator is connected with described main heat exchanger by the 20 pipeline 120.
Under described low-pressure, tower is operating pressure 0.2 ~ 0.22MPa, and under described high pressure, tower is operating pressure ~ 0.36MPa.
Under described high pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, under described low-pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, described upper tower to be the number of plates be 30 ~ 40 or corresponding tower tray number be 52 ~ 68 dishes structured packings on tower.
Take out two-part in high pressure air compressor machine band described in described low-pressure air compressor machine pressure at expulsion 0.25 ~ 0.27MPa., in take out pressure 0.38, last stage pressure ~ 0.65MPa, can according to different oxygen pressure operating mode, adjustment last stage pressure.
Embodiment two
Utilize the device of the low purity oxygen air separation described in embodiment one to carry out a method for oxygen air separation, the method is as follows:
Air is divided into three parts through the compression of low-pressure air compressor machine after front end precooling purifying: Part I air enters main heat exchanger, the gas that backflowed cooling laggard enter tower under low-pressure; The air that Part II is equivalent to swell increment enters the pressurized end supercharging of turbo-expander, after supercharging through cooler cooling laggard enter main heat exchanger, extract out in the middle part of main heat exchanger after being cooled to uniform temperature and enter decompressor, the air after expansion sends into upper tower; Part III air enters the compression of high pressure air compressor machine, extract out after a part enters main heat exchanger cooling and enter tower under high pressure, remainder compresses further through high pressure air compressor machine, liquid oxygen evaporator is entered as thermal source liquid oxygen vaporisation after main heat exchanger cooling, be divided into two strands after going out liquid oxygen evaporator: one enters under high pressure in the middle part of tower, another stock to enter under low-pressure in the middle part of tower; Air, after lower tower rectifying, obtains liquid air at lower tower bottom, obtains liquid nitrogen at top;
Wherein, under high pressure, tower produces liquid nitrogen, lean solution sky and oxygen-enriched liquid air from top to bottom, under oxygen-enriched liquid air throttling enters low-pressure, tower condenser is as low-temperature receiver, lean solution empty through subcooler cross cold after, throttling enters Shang Ta, as its phegma, pure liquid nitrogen is crossed top of tower in cold rear feeding and is made phegma in subcooler; Under low-pressure, tower produces liquid nitrogen and oxygen-enriched liquid air from top to bottom, under oxygen-enriched liquid air throttling enters low-pressure, tower condenser is as low-temperature receiver, liquid nitrogen is crossed top of tower in cold rear feeding and is made phegma in subcooler, and the liquid air vapo r under low-pressure after the evaporation of tower condenser is sent in the middle part of upper tower and participated in rectifying; Nitrogen and liquid oxygen is produced from top to bottom at upper tower, nitrogen extract out from upper top of tower after through subcooler and main heat exchanger re-heat to design temperature cooling box, one dirty nitrogen is used for the regeneration of molecular sieve adsorber, another stock is delivered to water-cooling tower and is cooled water, also have sub-fraction to enter ice chest, ice chest is inflated; Liquid oxygen is extracted out from upper tower bottom and is entered liquid oxygen evaporator, is heated by the air that vaporization is laggard to be entered to be sent to user after main heat exchanger re-heat to normal temperature.
The gas of decompressor pressurized end is from the gas after low-pressure air compressor machine.
Product oxygen purity 70% ~ 97%, product oxygen pressure 0.4bar(G) ~ 2bar(G), oxygen extraction ratio more than 99%.
The conventional double-column process of air separation unit observable index is low more than 10%.
The device of the low purity oxygen air separation mentioned in the present embodiment is identical with the device of the low purity oxygen air separation described in embodiment one, and this is no longer going to repeat them.

Claims (4)

1. the device of a low purity oxygen air separation, comprise air compression system, front end precooling purification system and ice chest, described air compression system comprises low-pressure air compressor machine and high pressure air compressor machine, described ice chest comprises main heat exchanger, liquid oxygen evaporator, the expanding end of decompressor and rectifying column, described rectifying column comprises tower under low-pressure, tower under high pressure, upper tower, tower condenser/evaporator and the condenser/evaporator under upper tower and high pressure between tower under low-pressure, it is characterized in that: described low-pressure air compressor machine is connected with front end precooling purification system by the first pipeline, first gas vent of described front end precooling purification system is connected with tower under described low-pressure through main heat exchanger by second pipe, second gas vent of front end precooling purification system is connected with the pressurized end of a decompressor by the 3rd pipeline, described pressurized end connects a water cooler by the 4th pipeline, and described water cooler is connected to the expanding end of described decompressor through main heat exchanger by the 5th pipeline, 3rd gas vent of described front end precooling purification system is connected with described high pressure air compressor machine by the 6th pipeline, and in high pressure air compressor machine, outlet port is connected with tower under described high pressure through main heat exchanger by the 7th pipeline, the outlet of high pressure air compressor machine final stage is connected with described liquid oxygen evaporator through main heat exchanger by the 8th pipeline, described liquid oxygen evaporator is connected to tower centre entrance place under described high pressure by the 9th pipeline and first throttle valve, and described liquid oxygen evaporator is connected to tower centre entrance place under described low-pressure by the tenth pipeline and second throttle, described expanding end outlet arranges the 11 pipeline and is connected with upper tower, under described high pressure, tower bottom liquid outlet is by being connected with described low-pressure tower condenser after the 12 pipeline and the 3rd choke valve, under described high pressure, tower central liquid exit connects the 13 pipeline, under described high pressure, the liquid outlet of top of tower connects the 14 pipeline, described 13 pipeline is connected to described upper tower centre entrance place after a subcooler and the 4th choke valve, and described 14 pipeline is connected to described upper top of tower porch after described subcooler and the 5th choke valve, under described low-pressure, tower bottom liquid outlet is connected with described low-pressure tower condenser by the 15 pipeline and the 6th choke valve, under described low-pressure, the liquid outlet of top of tower connects the 16 pipeline, described 16 pipeline is connected to the upper entrance place of described upper tower after described subcooler and the 7th choke valve, and under described low-pressure, the dirty nitrogen of tower condenser is connected with upper tower centre entrance by the 17 pipeline, the dirty nitrogen outlet place of described upper top of tower connects the 18 pipeline, and described 18 pipeline connects described subcooler and main heat exchanger, the liquid oxygen side outlet place of described condenser/evaporator is connected with described liquid oxygen evaporator by the 19 pipeline, and the gas oxygen outlet of described liquid oxygen evaporator is connected with described main heat exchanger by the 20 pipeline.
2. the device of a kind of low purity oxygen air separation according to claim 1, it is characterized in that: under described low-pressure, tower is operating pressure 0.2 ~ 0.22MPa, under described high pressure, tower is operating pressure ~ 0.36MPa.
3. the device of a kind of low purity oxygen air separation according to claim 1, it is characterized in that: under described high pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, under described low-pressure tower to be the number of plates be 25 ~ 35 or corresponding tower tray number be the lower towers of 35 ~ 50 dishes, described upper tower to be the number of plates be 30 ~ 40 or corresponding tower tray number be 52 ~ 68 dishes structured packings on tower.
4. the device of a kind of low purity oxygen air separation according to claim 1, it is characterized in that: in high pressure air compressor machine band described in described low-pressure air compressor machine pressure at expulsion 0.25 ~ 0.27MPa., take out two-part, in take out pressure 0.38, last stage pressure ~ 0.65MPa, can according to different oxygen pressure operating mode, adjustment last stage pressure.
CN201520593333.XU 2015-08-10 2015-08-10 Low -purity oxygen air separation's device Withdrawn - After Issue CN204923686U (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105115244A (en) * 2015-08-10 2015-12-02 开封空分集团有限公司 Low-purity oxygen air separating device and method
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

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105115244A (en) * 2015-08-10 2015-12-02 开封空分集团有限公司 Low-purity oxygen air separating device and method
CN105115244B (en) * 2015-08-10 2017-06-27 开封空分集团有限公司 The device and method that a kind of low purity oxygen air is separate
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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