CN100472159C - Air separating device and method therefor - Google Patents
Air separating device and method therefor Download PDFInfo
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- CN100472159C CN100472159C CN 200610020936 CN200610020936A CN100472159C CN 100472159 C CN100472159 C CN 100472159C CN 200610020936 CN200610020936 CN 200610020936 CN 200610020936 A CN200610020936 A CN 200610020936A CN 100472159 C CN100472159 C CN 100472159C
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
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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
- F25J3/04296—Claude expansion, i.e. expanded into the main or 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
- F25J3/04248—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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a method for using rectification at low temperature to separate air, and relative device. Wherein, said device comprises a booster (5), an expander (6), and a cooler (10) to form one low-temperature boost turbine expander, which will boost and cool another air to be reduced temperature, expanded and cooled in the main heat exchanger to be fed into the upper tower (14) of rectification tower for rectification. In the separation process, it uses different expanders as middle pressure and low pressure, which expand in different pressures and temperatures to supply cold energy to the separation process; the expanded air is fed into the upper and lower towers for rectification. The invention has lower unit electricity consumption as 2.5% reduced.
Description
Technical field
The present invention relates to a kind of method and apparatus of air separation, specially refer to the method and apparatus that utilizes rectifying to come separation of air at low temperatures.
Background technology
At present, utilizing rectifying to come the interior compression process of separation of air at low temperatures is a kind of known industrial production technology.Usual way is: the air of process compressor compresses cools off in chilldown system and remove steam in cleaning system, is divided into two strands of air-flows behind the objectionable impurities such as carbon dioxide.One air-flow is divided into two-way again after supercharging, cooling, one the tunnel enters ice chest after supercharging compression once more, cooling, tower under the main heat exchanger cooling is liquefied and sent into after step-down, flow with air as swell refrigeration on another road, its enters heat exchanger after supercharging and the water cooler cooling once more through decompressor supercharger, enter decompressor after reducing temperature, air externally does work, after the step-down cooling, cross heat exchanger with another stock-traders' know-how and cool near converging the bottom that enters tower under the rectifying column separating of saturation temperature with air stream.Rectifying column is made up of Xia Ta, last tower and condenser/evaporator.Air obtains initial gross separation at Xia Tazhong, obtains to contain the more oxygen-enriched liquid air of oxygen in the bottom, and oxygen-enriched liquid air is drawn down behind the tower through crossing the cold and a part of Shang Ta of entering of throttling expansion, and as the phegma of last tower, another part introducing crude argon column condenser is as low-temperature receiver.Proper site at following tower is extracted liquid nitrogen fraction out, participates in rectifying through sending into the tower proper site after cold and the throttling step-down as phegma.The top of following tower obtains nitrogen, few partly can be used as product after re-heat outside confession, condensation becomes liquid nitrogen to all the other nitrogen with the liquid oxygen heat exchange in condenser/evaporator.The part of this liquid nitrogen becomes the phegma of tower down, and another part liquid nitrogen enters Shang Ta through crossing cold major part through throttling expansion after being drawn condenser/evaporator, and as the phegma of last tower, few part also can be used as product and supplies outward.Bottom at last tower obtains liquid oxygen, the small part liquid oxygen can be used as product and draws, part liquid oxygen boosts to through liquid oxygen pump and draws as product after main heat exchanger heats up the vaporization re-heat after requiring pressure again, most liquid oxygen is heated as gas oxygen by nitrogen in condenser/evaporator, part gas oxygen also can be used as product outer confession after re-heat, and most gas oxygen is then as the ascending air participation rectifying of last tower.The top of last tower can obtain nitrogen, and top can obtain dirty nitrogen.Can also extract out at the suitable position of last tower and to contain the higher argon cut of argon, can obtain the product argon through rectifying at argon producing system.Adopt such method and apparatus to come separation of air to obtain oxygen, nitrogen and argon, particularly liquid oxygen, nitrogen product and pressure oxygen, the nitrogen product of different shape, the power consumption of unit product is higher.
Summary of the invention
The objective of the invention is to propose a kind of energy-conservation, the air-separating plant that operating cost is low.
In order to achieve the above object, the present invention adopts following technical scheme: a kind of air-separating plant comprises:
(1), air is pressurizeed and remove the compressor that objectionable impurities makes it to become raw air, chilldown system and cleaning system;
(2), supercharger, the cooler of the part material supercharging air after will purifying and middle pressure booster expansion turbine and high pressure booster compressor and the cooler that on this pressure-based, raw air is carried out supercharging, cooling, expansion;
(3), different fluids is carried out main heat exchanger, subcooler and the swelling heat exchanger of cold and hot exchange;
(4), will separate with raw air and carry out the rectifying column of separating obtained product and carry ar system, this rectifying column is by down tower, condenser/evaporator and go up tower and constitute;
Also comprise a low-pressure charging turbo-expander of forming by supercharger, decompressor and cooler, this low-pressure charging turbo-expander with another strand raw air through supercharging, cooling, and the back swell refrigeration of in main heat exchanger, lowering the temperature, the last tower of sending into then in the rectifying column participates in rectifying.
Another object of the present invention is to propose a kind of reduction power consumption, the air separation new method of saving operating cost.
In order to achieve the above object, the present invention adopts following technical scheme: (1), through compressor compresses, chilldown system cooling and in cleaning system, remove objectionable impurities after air split into separation and flowed with raw air with raw air stream and supercharging, supercharging is with the raw air supercharger of flowing through, cooling raw air stream of compression swelling and high pressure feedstock air stream in splitting into again after the cooler supercharging cooling, during flowing through, the middle cooling raw air of compression swelling presses the supercharger supercharging of booster expansion turbine, cooling is laggard in cooler goes into the main heat exchanger cooling, press the decompressor of booster expansion turbine to expand then in the warp, converge again with through the raw air stream in the main heat exchanger, enter the following tower rectifying in the rectifying column; Another burst high pressure feedstock air is through the supercharger supercharging, sends into following tower rectifying in the rectifying column again in the main heat exchanger cooling liquid after the choke valve step-down;
(2), separation is flowed with raw air and supercharging is flowed through by after tower, condenser/evaporator reach the rectifying column rectifying that upward tower constitutes down with raw air, is separated into the product liquid oxygen, nitrogen products and low pressure purity nitrogen, dirty nitrogen and argon cut;
Through compressor compresses, chilldown system cooling and in cleaning system, remove objectionable impurities after air also split into the cooling raw air stream of one inflated with low pressure, the supercharging in the supercharger of a low-pressure charging turbo-expander forming by supercharger, decompressor and cooler of flowing through of this raw air, cooling in cooler, the back swell refrigeration in decompressor of in main heat exchanger, lowering the temperature, the last tower of sending into then in the rectifying column participates in rectifying; In this air separating method, supercharger, decompressor and the cooler of the supercharger of low-pressure charging turbo-expander, decompressor and cooler and middle pressure booster expansion turbine are to start operation simultaneously, its objective is to cut down the consumption of energy.
Realize by following technical measures that in the present invention major technique feature of the present invention is:
In the compressed air separating process, low-pressure charging turbo-expander and middle pressure booster expansion turbine have been used.They make the raw air swell refrigeration under different pressure and temperatures, enter Shang Ta and following tower participation rectifying then respectively.
Through the air of compressor compresses in chilldown system, cool off and in cleaning system, remove objectionable impurities such as steam, acetylene and carbon dioxide after be divided into three strands of air-flows, one air-flow is through being divided into two-way again after supercharging, the cooling: the one tunnel enters ice chest after supercharging once more, cooling, and cooling is liquefied and send into tower down after step-down in main heat exchanger; Another road is as the swell refrigeration air-flow, its through in press booster expansion turbine supercharger supercharging and water cooler cooling are laggard once more goes into main heat exchanger, enter decompressor after reducing temperature, the external work done of air, cross the raw air that main heat exchanger cools near saturation temperature with second stock-traders' know-how after the decrease temperature and pressure and converge, the bottom that enters tower under the rectifying column participates in rectifying; The 3rd strand of raw air be through the supercharger supercharging of low-pressure charging turbo-expander, and the water cooler cooling is laggard goes into main heat exchanger, cools to enter decompressor after the uniform temperature and expand, and the air after the expansion is sent into tower participation rectifying.The air that enters down tower is after the preliminary rectifying of following tower, at the bottom of tower, obtain oxygen-enriched liquid air, oxygen-enriched liquid air is crossed through subcooler and is divided into two-way after cold: the one tunnel sends into the phegma of tower as last tower after the throttling step-down, the one tunnel sends into crude argon condenser as low-temperature receiver after the throttling step-down.The liquid nitrogen fraction that obtains in the following proper site of tower is sent into tower as phegma through after cold, the throttling step-down.Top at following tower obtains pure nitrogen gas, small part can be used as product and supplies outside after re-heat, all the other are condensed into liquid nitrogen with the liquid oxygen heat exchange in condenser/evaporator, the part of this liquid nitrogen becomes the phegma of tower down, another part liquid nitrogen is drawn condenser/evaporator after subcooler is cold excessively, small part can be used as the outer confession of product, and major part is sent into top of tower as phegma after the throttling step-down.Gas, liquid logistics are after the rectifying once more of last tower, bottom at last tower obtains liquid oxygen, part liquid oxygen is drawn as product, another part liquid oxygen boosts to through liquid oxygen pump and requires pressure after draw as product after the main heat exchanger intensification vaporization re-heat, most of liquid oxygen is heated as gas oxygen by nitrogen in condenser/evaporator, small part gas oxygen also can be used as product after re-heat outside confession, most of gas oxygen then participates in rectifying as the ascending air of last tower.The top of last tower can obtain nitrogen, and top can obtain dirty nitrogen, and they draw ice chest after re-heat in subcooler, swelling heat exchanger and main heat exchanger, remove the technology assigned address.Can also extract out at the suitable position of last tower and to contain the higher argon cut of argon, can obtain the product argon through rectifying at argon producing system.
In apparatus of the present invention, except that middle pressure booster expansion turbine provides the cold, also having increased a low-pressure charging turbo-expander provides cold.In the process of air separating method, in having used, the decompressor of these two kinds of different pressures grades of low pressure, two kinds of decompressors of mesolow expand under different pressure and temperatures, outwards work done, for air separation process provides cold, the air after the expansion enters upper and lower tower respectively and participates in rectifying.After the invention process abovementioned technology, it is about 2.5% that the unit power consumption of oxygen is descended, and for large-scale space division device, a year economize on electricity can reach millions of even up to ten million degree, and energy-saving effect is obvious.
Description of drawings
Fig. 1 structural principle flow chart of the present invention;
In Fig. 1,1 is booster compressor, and 3 is that supercharger, 4 is decompressor, 5 is that supercharger, 6 is decompressor, 2 is the high pressure booster compressor, and 7,8,9,10 is water cooler, and 11 is main heat exchanger, 12 are following tower, 13 is condenser/evaporator, and 14 is last tower, and 15 is subcooler, 16 is swelling heat exchanger, and 17 is liquid oxygen pump.Relevant material flow is made following numbering: 101 are raw air, the 102nd, directly advance the raw air of main heat exchanger, 103 are the supercharging raw air, 104 is middle pressure pressuring expansion air stream, 105 is the high pressure feedstock air-flow, 106 is the raw air stream that into descends tower bottom, and 107 is oxygen-enriched liquid air, and 108 for removing the oxygen-enriched liquid air of crude argon condenser, 109 for removing the oxygen-enriched liquid air of tower, 110 is liquid nitrogen fraction, and 111 is liquid nitrogen, and 112 for removing the liquid nitrogen of tower, 113 is nitrogen products, 114 is liquid oxygen, and 115 for compressing the liquid oxygen that boosts and heat up in going, and 116 is the product liquid oxygen, 117 is pure nitrogen gas, 118 is dirty nitrogen, and 119 is the argon cut, and 120 for removing the raw air of low-pressure charging turbo-expander.Wherein supercharger 3, decompressor 4, cooler 9 are pressed booster expansion turbine in constituting, and supercharger 5, decompressor 6, cooler 10 constitute the low-pressure charging turbo-expander.
The specific embodiment
The invention will be further described below in conjunction with accompanying drawing 1 and embodiment.
Cool off in chilldown system and the raw air 101 removed in cleaning system behind the objectionable impurities such as water vapour, acetylene and carbon dioxide is divided into three strands through the air of compressor compresses: first strand 103 is divided into two-way through booster compressor 1 compression, water cooler 7 again after cooling off, one the tunnel 105 goes into main heat exchanger 11 through the 2 further superchargings of high pressure supercharger, water cooler 8 coolings are laggard, in main heat exchanger, backflowed air cooling but and liquefaction, sent into down tower 12 suitable positions participations rectifying through the throttling step-down then.Press supercharger 3 superchargings of booster expansion turbine in another road 104 warps, after in water cooler 9, cooling off, enter main heat exchanger 11 and backflowed gas cooled to set point of temperature, press the decompressor 4 of booster expansion turbine to expand then in the warp, step-down cooling back is converged to the raw air stream 102 near saturation temperature with second burst of gas cooled of being backflowed in main heat exchanger 11, and the bottom that enters down tower 12 then participates in rectifying.120 superchargings in the supercharger 5 of low-pressure charging turbo-expander of the 3rd strand of raw air stream, cooling is laggard in water cooler 10 goes into main heat exchanger 11, the gas cooled of being backflowed goes decompressor 6 to expand after set point of temperature, enter swelling heat exchanger 16 after the step-down cooling, send into tower 14 suitable positions after the gas cooling of being backflowed and participate in rectifying.
Be divided into two-way after oxygen-enriched liquid air 107 mistake subcooler 15 of descending tower 12 bottoms to extract out is cold, the one tunnel 108 goes crude argon condenser as low-temperature receiver after the throttling step-down, and one the tunnel 109 enters tower 14 proper site after the throttling step-down become the phegma of going up tower 14.Second strand of phegma of tower 14 on the proper site of sending into tower 14 after, the throttling step-down cold through subcooler 15 from the liquid nitrogen fraction 110 that following tower 12 proper site are extracted out becomes with excessivelying.Nitrogen in tower 12 tops acquisition down is condensed into liquid nitrogen by liquid oxygen in condenser/evaporator 13, part liquid nitrogen becomes the phegma of tower down, other liquid nitrogen 111 is extracted out from condenser/evaporator 13 after subcooler 15 is cold excessively, be divided into two strands then, one is 113 as nitrogen products, and another strand 112 sent into tower 14 tops after the throttling step-down become the 3rd strand of phegma going up tower 14.The ascending air of tower 14 in condenser/evaporator 13, being become by the oxygen of nitrogen heating and gasifying, through exchanging with above-mentioned three strands of phegmas and through the caloic that decompressor 6 is sent into the air stream 120 of tower, obtain liquid oxygen in last tower 14 bottoms, part liquid oxygen 114 is extracted out as product, wherein 116 is liquid oxygen products, and 115 are gone the oxygen product of the required pressure of main heat exchanger 11 gasification re-heats becoming to send ice chest after liquid oxygen pump 17 boosts.The product nitrogen 117 that obtains at last tower 14 tops is sent ice chest after subcooler 15, main heat exchanger 11 re-heats.The dirty nitrogen 118 that obtains on last tower 14 tops is sent ice chest after subcooler 15, swelling heat exchanger 16 and main heat exchanger 11 re-heats, go to the technology precalculated position.
When needing to extract the argon product, also can contain the higher argon cut 119 of argon from the suitable position extraction of last tower 14.Ar system is an old process, with getting in touch of king-tower also be conventional, schematic diagram and the explanation in do not show.
What need stress is: the process organization of interior compression air separation plant can change.For example, when purity nitrogen output was high, the gas that backflows that removes swelling heat exchanger 16 may be purity nitrogen 117 rather than dirty nitrogen 118; Following tower 12 can not taken out liquid nitrogen fraction 110, and the part that will go out the high pressure liquid air 105 of main heat exchanger 11 is sent into down tower 12 through throttling, and a part is sent into tower 14 through throttling; Also available decompressor replaces sends into down tower 12 or the like after choke valve is used high pressure liquid air 105 step-downs of main heat exchanger 11.But change no matter which kind of flow process does,, just belong to the protection domain of this patent as long as the low-pressure charging turbo-expander in the flow process of interior compression air separation plant, occurs.
Claims (1)
1, a kind of application of air separator carries out the method for air separation, and wherein, air-separating plant comprises:
(1), air is pressurizeed and remove the compressor that objectionable impurities makes it to become raw air, chilldown system and cleaning system;
(2), the raw air supercharger (1) of the part material supercharging air after will purifying, raw air cooler (7) and the middle pressure booster expansion turbine (3,4,9) and high pressure booster compressor (2) and the high pressure cooling cooler (8) that on this pressure-based, raw air are carried out supercharging, cooling, expansion;
(3), different fluids is carried out main heat exchanger (11), subcooler (15) and the swelling heat exchanger (16) of cold and hot exchange;
(4), will separate with raw air and carry out the rectifying column of separating obtained product and carry ar system, this rectifying column is by down tower (12), condenser/evaporator (13) and go up tower (14) and constitute;
Also comprise a low-pressure charging turbo-expander of forming by low-pressure charging machine (5), low-pressure expansion machine (6) and low pressure cooler (10), this low-pressure charging turbo-expander with another strand raw air through supercharging, cooling, and the back swell refrigeration of in main heat exchanger, lowering the temperature, the last tower of sending into then in the rectifying column (14) participates in rectifying; Using described air-separating plant carries out air separating method and comprises the steps:
(a), through compressor compresses, chilldown system cooling and in cleaning system, remove objectionable impurities after air (101) split into separation with raw air stream (102) and supercharging with raw air stream (103), supercharging is flowed (103) through raw air supercharger (1) with raw air, cooling raw air stream of compression swelling (104) and high pressure feedstock air stream (105) in splitting into again after raw air cooler (7) the supercharging cooling, press supercharger (3) supercharging of booster expansion turbine in the middle cooling raw air stream of compression swelling (104) warp, cooling is laggard in middle pressure cooler (9) goes into main heat exchanger (11) cooling, press the decompressor (4) of booster expansion turbine to expand then in the warp, converge again with through flowing (102) with raw air separating in the main heat exchanger (11), enter following tower (12) rectifying in the rectifying column; Described high pressure feedstock air stream (105) is through high pressure booster compressor (2) supercharging, sends into following tower (12) rectifying in the rectifying column again in main heat exchanger (11) cooling liquid after the choke valve step-down;
(b), after separation reaches the rectifying column rectifying that upward tower (14) constitutes with raw air stream (103) via following tower (12), condenser/evaporator (13) with raw air stream (102) and supercharging, be separated into product liquid oxygen (114), nitrogen products (113) and low pressure purity nitrogen (117), dirty nitrogen (118) and argon cut (119);
It is characterized in that:
Through compressor compresses, chilldown system cooling and in cleaning system, remove objectionable impurities after air (101) also split into the cooling raw air stream of one inflated with low pressure (120), the cooling raw air stream of this inflated with low pressure (120) is via low-pressure charging machine (5), supercharging in the supercharger (5) of the low-pressure charging turbo-expander that low-pressure expansion machine (6) and low pressure cooler (10) are formed, cooling in low pressure cooler (10), cooling back swell refrigeration in low-pressure expansion machine (6) in main heat exchanger (11), the last tower of sending into then in the rectifying column (14) participates in rectifying; In this air separating method, the supercharger (3) of the supercharger of low-pressure charging turbo-expander (5), low-pressure expansion machine (6) and low pressure cooler (10) and middle pressure booster expansion turbine, middle-pressure expansion machine (4) and middle pressure cooler (9) are to start operation simultaneously.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| US9182170B2 (en) * | 2009-10-13 | 2015-11-10 | Praxair Technology, Inc. | Oxygen vaporization method and system |
| CN103361138B (en) * | 2013-07-24 | 2015-02-18 | 开封黄河空分集团有限公司 | Method for preparing liquefied natural gas and synthesis ammonia raw material gases by use of hydrogen extraction desorption gas |
| CN107421187A (en) * | 2017-08-22 | 2017-12-01 | 河南大学 | A kind of deep-sea fishing liquid air instant-frozen system |
| WO2019104524A1 (en) * | 2017-11-29 | 2019-06-06 | 乔治洛德方法研究和开发液化空气有限公司 | Cryogenic distillation method and apparatus for producing pressurized air by means of expander booster in linkage with nitrogen expander for braking |
| CN108240734B (en) * | 2018-03-08 | 2024-03-26 | 李佳晨 | Air supply system of booster expander and air separation equipment |
| JP6351895B1 (en) * | 2018-03-20 | 2018-07-04 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Nitrogen production method and nitrogen production apparatus |
| CN108413708A (en) * | 2018-06-14 | 2018-08-17 | 上海联风能源科技有限公司 | It is a kind of to improve the method and device for having space division liquid yield |
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| CN109470062A (en) * | 2018-11-02 | 2019-03-15 | 辽宁新瑞碳材料科技有限公司 | A kind of exhaust treatment system containing argon of high temperature furnace dry production graphite for diamond |
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| CN1865822A (en) | 2006-11-22 |
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Effective date of registration: 20180607 Address after: 063200 Caofeidian Industrial Zone, Tangshan City, Hebei Province, south of Sanya Road, eighteen plus head. Patentee after: Tangshan Ruixin Liquefied Gas Co., Ltd. Address before: No. 239 construction road, Jianyang City, Sichuan Province Patentee before: Sichuan Air Separation Plant (Group) Co., Ltd |