CN102032756A - Air separation method - Google Patents
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- CN102032756A CN102032756A CN2011100027585A CN201110002758A CN102032756A CN 102032756 A CN102032756 A CN 102032756A CN 2011100027585 A CN2011100027585 A CN 2011100027585A CN 201110002758 A CN201110002758 A CN 201110002758A CN 102032756 A CN102032756 A CN 102032756A
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Abstract
The invention relates to an air separation method. In the method, the pressures of an upper tower and a lower tower are improved, the refrigerating capacity of liquefied natural gas is used, and a reflux gas supercharged turbine expansion machine is also used. Compared with the similar technical scheme, the air separation technical scheme of the invention has the advantages that: energy consumption of a unit product can be reduced obviously; more liquid air separation products also can be produced under the same gasification capacity of the liquefied natural gas; and thus, recycling economy and energy conservation and emission reduction are realized.
Description
Technical field
The present invention relates to a kind of air separating method.
Background technology
Before the present invention proposes, because the condensing temperature very low (critical-temperature is-140.7 ℃) of air comes the method for separation of air to require the external world to provide lot of energy to obtain suitable cold by rectifying at low temperatures.Liquefied natural gas (being called for short LNG) is promoted the use of as clean fuel.The Main Ingredients and Appearance of liquefied natural gas is a methane, and the evaporating temperature under the normal pressure is about-160 ℃.Liquefied natural gas is acted as a fuel when using, must and be heated to normal temperature liquefied natural gas gasifying.If the cold of liquefied natural gas is applied in the air-separating plant goes, all be the good thing of killing two birds with one stone still to the use of liquefied natural gas to air separation.
From safety, often adopt nitrogen and liquefied natural gas to carry out the cold exchange.So the air separating method that utilizes cold energy of liquefied natural gas often adopts the mode of nitrogen circulation.In general, through overcompression and the clean raw air after purifying reach capacity by the cold exchange and enter rectifying column after temperature or part are with liquid.Rectifying column is made up of Xia Ta, last tower and main condenser evaporimeter.Raw air carries out initial gross separation at the following tower of rectifying column, obtains oxygen-enriched liquid air in its bottom.After being drawn, this oxygen-enriched liquid air enters Shang Ta as phegma through crossing the cold-peace throttling expansion.Top at following tower obtains gas nitrogen, and by the condensation of liquid oxygen institute, condensed a part of liquid nitrogen becomes the phegma of tower down to part gas nitrogen, goes after another part liquid nitrogen is drawn from condenser/evaporator to converge with the liquid nitrogen in another source in condenser/evaporator.Part gas nitrogen is drawn from the top of tower down after over-heat-exchanger is heated the rear section can be used as product and draw, remainder enters the nitrogen supercharging machine after then converging with another strand nitrogen, and the nitrogen that has improved pressure passes through and enters the liquefied natural gas heat exchanger after water cooler cools off.Nitrogen is cooled and is condensed into liquid nitrogen in this heat exchanger, and liquefied natural gas in this heat exchanger, obtain the gasification and be heated as natural gas after leave to use it for anything else.The liquid nitrogen that leaves heat exchanger enters gas-liquid separator through after the throttling expansion, the liquid nitrogen of separating merges with the liquid nitrogen of drawing from the main condenser evaporimeter, passed through cold back small part and can be used as product and draw, major part is then sent into the phegma of tower as last tower through after the throttling.The gas nitrogen of separating then returns the liquefied natural gas heat exchanger and is heated the back and converges the nitrogen supercharging machine that enters from what following tower was drawn through the heated gas nitrogen of heat exchanger, has finished nitrogen circulation.Tower bottom can obtain the gentle oxygen of liquid oxygen on rectifying column, can obtain returning polluted nitrogen (and nitrogen reflux) at the top.The cold of using liquefied natural gas comes the method and apparatus of separation of air, and the power consumption of unit product has bigger decline, but power consumption also has the leeway that reduces still than higher for the device of producing liquid oxygen and liquid nitrogen.
Summary of the invention
The lower air separating method of energy consumption that the purpose of this invention is to provide a kind of unit product.
For achieving the above object, the technical solution used in the present invention is:
A kind of air separating method comprises
In main heat exchanger, reach capacity after temperature or part be with liquid through compressor compresses and cooling in chilldown system, the air of in cleaning system, removing objectionable impurities, enter rectifying column and participate in rectifying by the cold exchange,
Rectifying column comprises Shang Ta, Xia Ta, main condenser evaporimeter,
The liquid oxygen that the bottom of tower obtains on described is crossed through liquid air subcooler and is drawn as product after cold; The nitrogen that is obtained by the top of described lower tower is divided into two-way; One road nitrogen is condensed into the liquid nitrogen rear portion at the main condenser evaporimeter and goes described lower tower to participate in rectifying; Another part is crossed through liquid nitrogen subcooler and is gone after cold described upper tower to participate in rectifying or cross cold supply outside as product afterwards through liquid nitrogen after cooler; Another road nitrogen returns lower tower participation rectifying or converges with the liquid nitrogen that goes out the main condenser evaporimeter after the nitrogen condenser/evaporator is condensed into liquid nitrogen
The oxygen-enriched liquid air that obtains by the bottom of described down tower through liquid air subcooler cross cold after, entering the described tower of going up through throttling expansion becomes phegma,
The dirty gas nitrogen that is obtained by described top of going up tower enters returning polluted nitrogen decompressor swell refrigeration after through the preliminary re-heat of dirty gas nitrogen, then through going to the technology precalculated position after the further re-heat of dirty gas nitrogen.
Preferably, at least one in the described liquid nitrogen subcooler of described dirty gas nitrogen process, liquid air subcooler, the main heat exchanger finished the preliminary re-heat of described dirty gas nitrogen.
Preferably, described dirty gas nitrogen is through behind the described returning polluted nitrogen decompressor, and at least one in the described liquid nitrogen subcooler of process, liquid air subcooler, the main heat exchanger finished the further re-heat of described dirty gas nitrogen.
Preferably, the pure gas nitrogen that is obtained by described top of going up tower enters pure gas nitrogen decompressor swell refrigeration after through the preliminary re-heat of pure gas nitrogen, then through releasing as product after the further re-heat of pure gas nitrogen.
Preferably, at least one in the described liquid nitrogen subcooler of described pure gas nitrogen process, liquid air subcooler, the main heat exchanger finished the preliminary re-heat of described pure gas nitrogen.
Preferably, described pure gas nitrogen is finished the further re-heat of described pure gas nitrogen through behind the described pure gas nitrogen decompressor through described liquid nitrogen subcooler, liquid air subcooler, main heat exchanger, at least one in cooler of liquid nitrogen.
Preferably, described air separating method provides institute's chilling requirement by liquefied natural gas, and described air separating method comprises the sealing nitrogen circulation, and described sealing nitrogen circulation is passed to the cold of described liquefied natural gas in the rectifying device; At least a portion of the nitrogen that is obtained by the top of described down tower goes described tower down to participate in rectifying after through the condensation of nitrogen condenser/evaporator, nitrogen in the described sealing nitrogen circulation carries out becoming liquid nitrogen after exchange heat and the cooling of process nitrogen liquefaction subcooler with liquefied natural gas in the liquefied natural gas heat exchanger, the liquid nitrogen that obtains after throttling carries out exchange heat through a nitrogen condenser/evaporator and a part that obtains nitrogen by the described top of tower down again, in main heat exchanger, gasified after the exchange heat, finished described sealing nitrogen circulation to being converted into the nitrogen in the sealing nitrogen circulation behind the nitrogen again.
Preferably, the liquid nitrogen that obtains of a part of throttling of the liquid nitrogen that is cooled to through nitrogen liquefaction subcooler obtains sealing nitrogen or gas nitrogen in the nitrogen circulation through liquefy one section compression entering the cryogenic nitrogen press after subcooler, the re-heat of liquefied natural gas heat exchanger converge for air inlet nitrogen with the nitrogen that is cooled to set point of temperature in the liquefied natural gas heat exchanger after the set point of temperature of nitrogen; Or the liquid nitrogen that obtains of a part of throttling of liquid nitrogen through nitrogen liquefy subcooler, the re-heat of liquefied natural gas heat exchanger after the set point of temperature with through after one section compression of cryogenic nitrogen press and two sections compressions that after the gas nitrogen that the liquefied natural gas heat exchanger is cooled to set point of temperature converges for air inlet nitrogen, enter the cryogenic nitrogen press obtain sealing nitrogen in the nitrogen circulation; Described cryogenic nitrogen press is one or two oil-free lubrication piston compressors or turbocompressor, the temperature of two sections air inlet nitrogen of one section air inlet nitrogen of described cryogenic nitrogen press, described cryogenic nitrogen press is lower than-80 ℃, and the nitrogen gas pressure in the sealing nitrogen circulation is greater than 3.4MPa.
Preferably, described air separating method also comprises the precool heat exchanger device, described liquefied natural gas is through behind the described liquefied natural gas heat exchanger, gasified and is heated to cooling medium generation heat exchange in described precool heat exchanger device and send more than 0 ℃ as combustion gas; Described cooling medium is recirculated cooling water or glycol water.
Preferably, the operating pressure (gauge pressure) of described tower down is greater than 0.65MPa, and the described operating pressure (gauge pressure) of tower of going up is greater than 0.07MPa.
Because technique scheme utilization, the present invention compared with prior art has following advantage: air separation technology scheme of the present invention is compared with similar technical scheme, the energy consumption of unit product is obviously reduced, the output of liquid space division product be can under the prerequisite of using same cold energy of liquefied natural gas, increase, recycling economy and energy-saving and emission-reduction realized.
Description of drawings
Accompanying drawing 1 is the schematic diagram of the embodiment one of air separating method of the present invention.
Accompanying drawing 2 is the schematic diagram of the embodiment two of air separating method of the present invention.
In the above accompanying drawing: 1, main heat exchanger; 2, Xia Ta; 3, main condenser evaporimeter; 4, Shang Ta; 5, liquid nitrogen subcooler; 6, liquid air subcooler; 7, nitrogen condenser/evaporator; 8, returning polluted nitrogen decompressor; 9, pure gas nitrogen decompressor; 10, liquid nitrogen is after cooler; 11, liquefied natural gas heat exchanger; 12, nitrogen liquefaction subcooler; 13, one of the cryogenic nitrogen press section; 14, two of the cryogenic nitrogen press sections; 15, precool heat exchanger device;
101, through cooling, cleaned air passes; 102, oxygen-enriched liquid air; 103, liquid nitrogen; 104, liquid nitrogen; 105, participate in the liquid nitrogen of rectifying; 106, nitrogen products; 107, nitrogen; 108, nitrogen; 109, nitrogen; 110, product liquid oxygen; 111, pure gas nitrogen; 112, dirty gas nitrogen; 113, the dirty gas nitrogen through expanding; 114, the pure gas nitrogen through expanding; 115, argon cut; 116, liquid nitrogen;
201, nitrogen; 202, air inlet nitrogen; 203, gas nitrogen; 204, the liquid nitrogen that obtains of throttling; 205, the liquid nitrogen that obtains of throttling; 206, air inlet nitrogen; 207, the nitrogen in the sealing nitrogen circulation; 208, liquid nitrogen; 209, the liquid nitrogen that obtains of throttling;
301, liquefied natural gas;
401, glycol water or recirculated cooling water.
The specific embodiment
Below in conjunction with embodiment shown in the drawings the present invention is further described.
Embodiment one: shown in accompanying drawing 1.
A kind of air separating method feeds rectifying in the rectifying column that comprises tower 4, following tower 2, main condenser evaporimeter 3 with air, obtains products such as liquid oxygen, liquid nitrogen, liquid argon.
In main heat exchanger 1, reach capacity after temperature or part be with liquid through compressor compresses and cooling in chilldown system, the air 101 of in cleaning system, removing objectionable impurities such as water vapour, carbon dioxide, enter rectifying column and participate in rectifying by the cold exchange.
The nitrogen 107 that is obtained by the following top of tower is divided into two parts, and a part of nitrogen 108 enters and is condensed into liquid nitrogen 116 in the main condenser evaporimeter 3, and another part nitrogen 109 participates in getting back to after the energy exchange time tower 2 cold is passed in the rectifying column in nitrogen condenser/evaporator 7.Liquid nitrogen 116 is divided into two-way, one road liquid nitrogen 103 goes down tower 2 to participate in rectifying, another road liquid nitrogen 104 through liquid nitrogen subcooler 5 cross cold after, a part becomes the liquid nitrogen 105 that participates in rectifying and goes tower 4 to participate in rectifying, another part nitrogen products 106 is crossed after cooler 10 through liquid nitrogen and is supplied outside as product after cold.
Draw as product behind liquid air subcooler 6 at the product liquid oxygen 110 that the bottom of last tower 4 obtains.The oxygen-enriched liquid air 102 that obtains by the following bottom of tower 2 through liquid air subcooler 6 cross cold after, entering tower 4 through throttling expansion becomes phegma.
This air separating method comprises the sealing nitrogen circulation, and the sealing nitrogen circulation is passed to the cold of liquefied natural gas 301 in the rectifying device.Nitrogen 207 in the sealing nitrogen circulation carries out becoming liquid nitrogen 208 after exchange heat and 12 coolings of process nitrogen liquefaction subcooler with liquefied natural gas 301 in liquefied natural gas heat exchanger 11, the liquid nitrogen 209 that liquid nitrogen 208 obtains after throttling passes through nitrogen condenser/evaporator 7 again and carries out exchange heat by the top acquisition nitrogen 109 that descends tower 2, be nitrogen 201 by gasification after the exchange heat in main heat exchanger 1, nitrogen 201 is cooled to set point of temperature through liquefied natural gas heat exchanger 11.The liquid nitrogen 204 that a part of throttling of liquid nitrogen 208 obtains enters the cryogenic nitrogen press after nitrogen liquefaction subcooler 12,11 re-heats of liquefied natural gas heat exchanger converge for air inlet nitrogen 202 with nitrogen 201 after the set point of temperature one section 13 compression obtains gas nitrogen 203.The liquid nitrogen 205 that a part of throttling of liquid nitrogen 208 obtains enters the cryogenic nitrogen press after nitrogen liquefaction subcooler 12,11 re-heats of liquefied natural gas heat exchanger converge for air inlet nitrogen 206 with the gas nitrogen 203 that is cooled to set point of temperature in liquefied natural gas heat exchanger 11 after the set point of temperature two section 14 compression obtains sealing the nitrogen 207 in the nitrogen circulation, finishes the sealing nitrogen circulation.The cryogenic nitrogen press is one or two oil-free lubrication piston compressors or turbocompressor, the temperature of one section 13 air inlet nitrogen 202 of cryogenic nitrogen press, two section 14 air inlet nitrogen 206 of cryogenic nitrogen press is lower than-80 ℃, the pressure of the nitrogen 207 in the sealing nitrogen circulation promptly should surpass the critical pressure of nitrogen greater than 3.4MPa.
Liquefied natural gas 301 through liquefied natural gas heat exchangers 11 after, with glycol water or recirculated cooling water 401 heat exchanges take place and gasified and be heated to more than 0 ℃ and send as combustion gas in precool heat exchanger device 15.Cooled glycol water or recirculated cooling water 401 send raw material air compressor machine intercooler and aftercooler as cooling medium, and implement circulation by pump.
The dirty gas nitrogen 112 that is obtained by the top of last tower 4 enters returning polluted nitrogen decompressor 8 swell refrigerations through liquid nitrogen subcooler 5, liquid air subcooler 6 after finishing the preliminary re-heat of dirty gas nitrogen successively, become the dirty gas nitrogen 113 through expanding, the dirty gas nitrogen 113 through expanding goes to the technology precalculated position through liquid air subcooler 6, main heat exchanger 1 after finishing the further re-heat of dirty gas nitrogen successively.
After finishing the preliminary re-heat of pure gas nitrogen through liquid nitrogen subcoolers 5, the pure gas nitrogen 111 that is obtained by the top of last tower 4 enters pure gas nitrogen decompressor 9 swell refrigerations, become the pure gas nitrogen 114 through expanding, the pure gas nitrogen 114 through expanding is released as product after finishing the further re-heat of pure gas nitrogen after cooler 10, process liquid nitrogen subcooler 5, liquid air subcooler 6, main heat exchanger 1 through liquid nitrogen successively.
Dirty gas nitrogen 112, pure gas nitrogen 111 are carried out swell refrigeration, can under the situation of identical liquefied natural gas gasifying amount, produce more liquid space division product, promptly reduced the energy consumption of unit product.
Can extract out in the appropriate location of last tower 4 and to contain the higher argon cut 115 of argon and go argon producing system to make the argon product.Technical scheme of the present invention is not limited to and only produces liquid oxygen, liquid nitrogen and liquid argon product.If desired, the gas of production part simultaneously oxygen, pressure gas nitrogen product or interior compressed oxygen, nitrogen, argon product.
The operating pressure of following tower 2 (gauge pressure) is greater than 0.65MPa, and the operating pressure of last tower 4 (gauge pressure) is greater than 0.07MPa.
Technical scheme of the present invention can also be used for single high nitrogen tower and only produce the gentle nitrogen product of liquid nitrogen product.
In the technical scheme of the present invention, whether one section 13 of the cryogenic nitrogen press, the correct position of two section 14 import and export pipe of cryogenic nitrogen press can be provided with hydrocarbon On-line Control instrument, can monitor liquefied natural gas 301 and leak in this sealing nitrogen circulation.Because this sealing nitrogen circulation and rectifier unit be relative closure also, can avoid liquefied natural gas 301 to leak in the rectifier unit and the danger that brings has improved security.
Embodiment two: shown in accompanying drawing 2.
A kind of air separating method feeds rectifying in the rectifying column that comprises tower 4, following tower 2, main condenser evaporimeter 3 with air, obtains products such as liquid oxygen, liquid nitrogen, liquid argon.
In main heat exchanger 1, reach capacity after temperature or part be with liquid through compressor compresses and cooling in chilldown system, the air 101 of in cleaning system, removing objectionable impurities such as water vapour, carbon dioxide, enter rectifying column and participate in rectifying by the cold exchange.
Nitrogen 107 by the top acquisition of tower down is divided into two parts, and a part of nitrogen 108 enters and is condensed into liquid nitrogen 116 in the main condenser evaporimeter 3, converges with the liquid nitrogen 116 that goes out main condenser evaporimeter 3 after another part nitrogen 109 is condensed in nitrogen condenser/evaporator 7.Liquid nitrogen 116 is divided into two-way, one road liquid nitrogen 103 goes down tower 2 to participate in rectifying, another road liquid nitrogen 104 is after liquid nitrogen subcooler 5 mistakes are cold, and a part becomes the liquid nitrogen 105 that participates in rectifying and goes tower 4 to participate in rectifying, and another part nitrogen products 106 supplies outward as product through after the throttling again.
Draw as product behind liquid air subcooler 6 at the product liquid oxygen 110 that the bottom of last tower 4 obtains.The oxygen-enriched liquid air 102 that obtains by the following bottom of tower 2 through liquid air subcooler 6 cross cold after, entering tower 4 through throttling expansion becomes phegma.
This air separating method comprises the sealing nitrogen circulation, and the sealing nitrogen circulation is passed to the cold of liquefied natural gas 301 in the rectifying device.Nitrogen 207 in the sealing nitrogen circulation carries out becoming liquid nitrogen 208 after exchange heat and 12 coolings of process nitrogen liquefaction subcooler with liquefied natural gas 301 in liquefied natural gas heat exchanger 11, the liquid nitrogen 209 that liquid nitrogen 208 obtains after throttling passes through nitrogen condenser/evaporator 7 again and carries out exchange heat by the top acquisition nitrogen 109 that descends tower 2, be nitrogen 201 by gasification again in main heat exchanger 1, nitrogen 201 is cooled to set point of temperature through liquefied natural gas heat exchanger 11.The liquid nitrogen 204 that a part of throttling of liquid nitrogen 208 obtains enters the cryogenic nitrogen press after nitrogen liquefaction subcooler 12,11 re-heats of liquefied natural gas heat exchanger converge for air inlet nitrogen 202 with nitrogen 201 after the set point of temperature one section 13 compression, obtain sealing the nitrogen 207 in the nitrogen circulation, finish the sealing nitrogen circulation.The cryogenic nitrogen press is oil-free lubrication piston compressor or turbocompressor, and the temperature of one section 13 air inlet nitrogen 202 of cryogenic nitrogen press is lower than-80 ℃, and the pressure of the nitrogen 207 in the sealing nitrogen circulation promptly should surpass the critical pressure of nitrogen greater than 3.4MPa.
Liquefied natural gas 301 is gasified and is heated to more than 0 ℃ through liquefied natural gas heat exchanger 11 to be sent as combustion gas.
The dirty gas nitrogen 112 that is obtained by the top of last tower 4 enters returning polluted nitrogen decompressor 8 swell refrigerations through liquid nitrogen subcooler 5, liquid air subcooler 6 after finishing the preliminary re-heat of dirty gas nitrogen successively, become the dirty gas nitrogen 113 through expanding, the dirty gas nitrogen 113 through expanding goes to the technology precalculated position through liquid air subcooler 6, main heat exchanger 1 after finishing the further re-heat of dirty gas nitrogen successively.Dirty gas nitrogen 112 is carried out swell refrigeration, can under the situation of identical liquefied natural gas gasifying amount, produce more liquid space division product, promptly reduced the energy consumption of unit product.
Release as product through liquid nitrogen subcoolers 5 liquid air subcoolers 6, main heat exchanger 1 back by the pure gas nitrogen 111 that the top of last tower 4 obtains.
Can extract out in the appropriate location of last tower 4 and to contain the higher argon cut 115 of argon and go argon producing system to make the argon product.
In the technical scheme of the present invention, last tower 4 can not go out pure gas nitrogen 111, only goes out dirty gas nitrogen 112.
The operating pressure of following tower 2 (gauge pressure) is greater than 0.65MPa, and the operating pressure of last tower 4 (gauge pressure) is greater than 0.07MPa.
Technical scheme of the present invention can also be used for single high nitrogen tower and only produce the gentle nitrogen product of liquid nitrogen product.
Whether in the technical scheme of the present invention, the correct position of one section 13 import and export pipe of cryogenic nitrogen press can be provided with hydrocarbon On-line Control instrument, can monitor liquefied natural gas 301 and leak in this sealing nitrogen circulation.Because this sealing nitrogen circulation and rectifier unit be relative closure also, can avoid liquefied natural gas 301 to leak in the rectifier unit and the danger that brings has improved security.
The foregoing description only is explanation technical conceive of the present invention and characteristics, and its purpose is to allow the personage who is familiar with this technology can understand content of the present invention and enforcement according to this, can not limit protection scope of the present invention with this.All the equivalence done of spirit essence changes or modifies according to the present invention, and for example the change etc. of crossing cooling method of product liquid oxygen, liquid nitrogen all should be encompassed within protection scope of the present invention.
Claims (10)
1. an air separating method comprises
In main heat exchanger (1), reach capacity after temperature or part be with liquid through compressor compresses and cooling in chilldown system, the air (101) of in cleaning system, removing objectionable impurities, enter rectifying column and participate in rectifying by the cold exchange,
Rectifying column comprises tower (4), following tower (2), main condenser evaporimeter (3),
The liquid oxygen (110) that the bottom of tower (4) obtains on described is crossed through liquid air subcooler (6) and is drawn as product after cold, the nitrogen (107) that is obtained by the top of described down tower is divided into two-way, one road nitrogen (108) is condensed into liquid nitrogen (a 116) back part at main condenser evaporimeter (3) and goes described tower (2) down to participate in rectifying, another part is crossed through liquid nitrogen subcooler (5) and is gone after cold the described tower (4) of going up to participate in rectifying or cross cold back through liquid nitrogen after cooler (10) supplying outside as product, another road nitrogen (109) returns down after nitrogen condenser/evaporator (7) is condensed into liquid nitrogen, and tower (2) participates in rectifying or converges with the liquid nitrogen that goes out main condenser evaporimeter (3) (116)
The oxygen-enriched liquid air (102) that obtains by the bottom of described down tower (2) through liquid air subcooler (6) cross cold after, entering the described tower (4) of going up through throttling expansion becomes phegma,
It is characterized in that: the dirty gas nitrogen (112) that is obtained by described top of going up tower (4) enters returning polluted nitrogen decompressor (8) swell refrigeration after through the preliminary re-heat of dirty gas nitrogen, then through going to the technology precalculated position after the further re-heat of dirty gas nitrogen.
2. air separating method according to claim 1 is characterized in that: at least one in described dirty gas nitrogen (112) process described liquid nitrogen subcooler (5), liquid air subcooler (6), the main heat exchanger (1) finished the preliminary re-heat of described dirty gas nitrogen.
3. air separating method according to claim 1, it is characterized in that: behind described dirty gas nitrogen (112) the described returning polluted nitrogen decompressor of process (8), at least one in process described liquid nitrogen subcooler (5), liquid air subcooler (6), the main heat exchanger (1) finished the further re-heat of described dirty gas nitrogen.
4. air separating method according to claim 1, it is characterized in that: the pure gas nitrogen (111) that is obtained by described top of going up tower (4) enters pure gas nitrogen decompressor (9) swell refrigeration after through the preliminary re-heat of pure gas nitrogen, then through releasing as product after the further re-heat of pure gas nitrogen.
5. air separating method according to claim 4 is characterized in that: at least one in described pure gas nitrogen (111) process described liquid nitrogen subcooler (5), liquid air subcooler (6), the main heat exchanger (1) finished the preliminary re-heat of described pure gas nitrogen.
6. air separating method according to claim 4, it is characterized in that: behind described pure gas nitrogen (111) the described pure gas nitrogen decompressor of process (9), finish the further re-heat of described pure gas nitrogen through described liquid nitrogen subcooler (5), liquid air subcooler (6), main heat exchanger (1), at least one in cooler (10) of liquid nitrogen.
7. air separating method according to claim 1, it is characterized in that: described air separating method provides institute's chilling requirement by liquefied natural gas (301), described air separating method comprises the sealing nitrogen circulation, and described sealing nitrogen circulation is passed to the cold of described liquefied natural gas (301) in the rectifying device; At least a portion of the nitrogen (107) that is obtained by the top of described down tower goes described tower (2) down to participate in rectifying after through nitrogen condenser/evaporator (7) condensation, nitrogen (207) in the described sealing nitrogen circulation carries out becoming liquid nitrogen (208) after exchange heat and process nitrogen liquefaction subcooler (12) cooling with liquefied natural gas (301) in liquefied natural gas heat exchanger (11), the liquid nitrogen that obtains after throttling (209) passes through nitrogen condenser/evaporator (7) again and carries out exchange heat with a part that obtains nitrogen (107) by the described top of tower (2) down, in main heat exchanger (1), gasified after the exchange heat, finished described sealing nitrogen circulation to being converted into the nitrogen (207) in the sealing nitrogen circulation behind the nitrogen (201) again.
8. air separating method according to claim 7 is characterized in that: the liquid nitrogen (204) that a part of throttling of the liquid nitrogen (208) that is cooled to through nitrogen liquefaction subcooler (12) obtains enters the cryogenic nitrogen press after nitrogen liquefaction subcooler (12), liquefied natural gas heat exchanger (11) re-heat converge for air inlet nitrogen (202) with the nitrogen (201) that is cooled to set point of temperature in liquefied natural gas heat exchanger (11) after the set point of temperature one section (13) compression obtains sealing nitrogen (207) or the gas nitrogen (203) in the nitrogen circulation; Or the liquid nitrogen (205) that obtains of a part of throttling of liquid nitrogen (208) through nitrogen liquefaction subcooler (12), liquefied natural gas heat exchanger (11) re-heat after the set point of temperature with through one section (13) of cryogenic nitrogen press compression back and two sections (14) after the gas nitrogen (203) that liquefied natural gas heat exchanger (11) is cooled to set point of temperature converges for air inlet nitrogen (206), entering the cryogenic nitrogen press compress the nitrogen (207) that obtains sealing in the nitrogen circulation; Described cryogenic nitrogen press is one or two oil-free lubrication piston compressors or turbocompressor, the temperature of the air inlet nitrogen (206) of two sections (14) of the air inlet nitrogen (202) of one section (13) of described cryogenic nitrogen press, described cryogenic nitrogen press is lower than-80 ℃, and the pressure of the nitrogen (207) in the sealing nitrogen circulation is greater than 3.4MPa.
9. air separating method according to claim 7, it is characterized in that: described air separating method also comprises precool heat exchanger device (15), described liquefied natural gas (301) through described liquefied natural gas heat exchanger (11) after, with cooling medium (401) heat exchange takes place and gasified and be heated to and send more than 0 ℃ as combustion gas in described precool heat exchanger device (15); Described cooling medium (401) is recirculated cooling water or glycol water.
10. air separating method according to claim 1 is characterized in that: the operating pressure (gauge pressure) of described tower (2) down is greater than 0.65MPa, and the described operating pressure (gauge pressure) of tower (4) of going up is greater than 0.07MPa.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103148676A (en) * | 2013-01-27 | 2013-06-12 | 南京瑞柯徕姆环保科技有限公司 | Air separation device for preparing oxygen and nitrogen through isobaric separation |
| CN107166872A (en) * | 2017-04-27 | 2017-09-15 | 杭州颐氧健康科技有限公司 | Health care gas deep cooling auto-pressurizing device for making and its method |
| CN110701870A (en) * | 2019-05-29 | 2020-01-17 | 苏州市兴鲁空分设备科技发展有限公司 | Air separation device and method utilizing LNG cold energy |
| CN112781321A (en) * | 2020-12-31 | 2021-05-11 | 乔治洛德方法研究和开发液化空气有限公司 | Air separation device with nitrogen liquefier and method |
| CN113562701A (en) * | 2021-09-18 | 2021-10-29 | 杭州制氧机集团股份有限公司 | Device and method for recovering byproduct oxygen from hydrogen production by water electrolysis by using low-temperature method |
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Application publication date: 20110427 |