CN1789868A - Air separating method by utilizing liquefied natural gas - Google Patents
Air separating method by utilizing liquefied natural gas Download PDFInfo
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- CN1789868A CN1789868A CN 200510022599 CN200510022599A CN1789868A CN 1789868 A CN1789868 A CN 1789868A CN 200510022599 CN200510022599 CN 200510022599 CN 200510022599 A CN200510022599 A CN 200510022599A CN 1789868 A CN1789868 A CN 1789868A
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- nitrogen
- natural gas
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- gas
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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
- F25J3/04151—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
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
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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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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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
Abstract
This invention relates to air isolation method by use of natural gas, which comprises the following steps: During air isolation process, using nitrogen gas as medium to send natural gas cold volume into entrance device to get each status oxidation, nitrogen gas product; Liquid natural gas is heated by gas; Adding extra cold load into the device to Directly supply low temperature liquid.
Description
Technical field
The present invention relates to a kind of air separating method, specially refer to the air separating method that utilizes cold energy of liquefied natural gas.
Background technology
Before the present invention proposes, because the condensing temperature very low (critical-temperature is-140.7 ℃) of air comes the method and apparatus of separation of air just 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, 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 by following tower, and last tower and condenser/evaporator are formed.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 another strand liquid nitrogen in condenser/evaporator.Part gas nitrogen is drawn from the top of tower down, converges the nitrogen supercharging machine that enters with another strand nitrogen after the over-heat-exchanger re-heat, and the nitrogen that has improved pressure is gone into the liquefied natural gas heat exchanger through supercooling is laggard.Nitrogen is cooled or is condensed into liquid nitrogen in this heat exchanger, and liquefied natural gas obtains gasification in the liquefied natural gas heat exchanger and re-heat becomes natural gas and leaves to use it for anything else.The 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 condenser/evaporator, 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 converges the nitrogen supercharging machine that enters with the gas nitrogen through the heat exchanger re-heat of drawing from following tower after then returning the re-heat of liquefied natural gas 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.
In this air separating method, the supply of liquefied natural gas is a vital thing.The production process of air separation is the industrial processes that continuity is very strong, needs the maintenance long-term operation continuously, arbitrarily start-stop car and increasing and decreasing load significantly except having a power failure and breaking down.In case liquefied natural gas is under-supply, even stop air feed, will cause the production process of air separation that frequent increasing and decreasing load and start-stop car take place, the production process utmost point not Steady is fixed.The cost of unit product will rise significantly, and economic benefit of enterprises will descend significantly.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of new air separating method that utilizes liquefied natural gas, and when liquefied natural gas was under-supply, the production process of air separation still can be moved continuously, and the cost of guarantor unit's product descends significantly.
The present invention is achieved by the following technical measures.In utilizing the air separation process of liquefied natural gas, add extra cold carrier.
Described extra cold carrier is the cryogenic liquid that is directly provided by the external world.
Through compressor compresses and cooling and in cleaning system, remove water vapour in chilldown system, raw air behind the objectionable impurities such as carbon dioxide enters main heat exchanger, after cooling to Eat and temperature or partly being with liquid, enter the bottom of the following tower of rectifying column, become the ascending air of tower down, fall the abundant contact of liquid stream in the column plate up and down and carry out the exchange of heat and quality.Bottom at following tower obtains to contain the more oxygen-enriched liquid air of oxygen.After this oxygen-enriched liquid air was drawn down tower, cold excessively by the returning polluted nitrogen that is come by last top of tower (and nitrogen reflux) through liquid air subcooler earlier, entering Shang Ta through throttling expansion again became one of phegma of going up tower.Top at following tower obtains nitrogen, and a part of nitrogen converges the back as nitrogen cycle with another strand nitrogen after the re-heat in main heat exchanger; The phegma of tower under a part of liquid nitrogen becomes after the condensation in the condenser/evaporator of another part nitrogen between Liang Ta, another part with converge from the liquid nitrogen of gas-liquid separator after cold excessively through liquid nitrogen subcooler by the returning polluted nitrogen (and nitrogen reflux) that comes by last top of tower, small part supplies outward as product; The top that the throttling expansion of most of process enters tower becomes another strand phegma of going up tower.Above-mentioned two strands of phegmas become the decline liquid stream of going up tower.Decline liquid stream fully contacts the exchange of carrying out heat and quality with ascending air on column plate.Bottom at last tower obtains liquid oxygen, and small part can be used as product and supplies outward.Most of liquid oxygen then is heated into gas oxygen by gas nitrogen in the condenser/evaporator between Liang Ta, and this gas oxygen becomes the ascending air of going up tower, also can extract small part gas oxygen after re-heat as supplying outside the product.Can obtain returning polluted nitrogen (and nitrogen reflux) at the top of last tower, the re-heat in liquid nitrogen subcooler and liquid air subcooler earlier of this portion gas enters the technology precalculated position after entering the main heat exchanger re-heat again.
The nitrogen of drawing by following top of tower through the main heat exchanger re-heat after with join from gas-liquid separator and through the nitrogen of re-heat, together enter the supercharging of nitrogen supercharging machine and in heat exchanger, cool off.These nitrogen enter liquefied natural gas heat exchanger and liquefied natural gas heat exchange cooling subsequently.Liquefied natural gas obtains gasification in the liquefied natural gas heat exchanger and re-heat is left to use it for anything else after becoming natural gas.The nitrogen that leaves the liquefied natural gas heat exchanger carries out entering gas-liquid separator after the throttling expansion, and the liquid nitrogen that is flowed out by gas-liquid separator converges with the liquid nitrogen from condenser/evaporator, again through liquid nitrogen subcooler cross cold after, a part can be used as product and supplies outward; Major part enters Shang Ta as phegma after throttling expansion.The gas nitrogen that is obtained by gas-liquid separator removes supercharger with being drawn by top of tower down to join through the nitrogen after the main heat exchanger re-heat in the liquefied natural gas heat exchanger after the re-heat, has finished nitrogen circulation.Directly provide extra cryogenic liquid to use by the external world as the cold carrier to device, to remedy because the cold that the liquefied natural gas supply is lacked when not enough.These extra cryogenic liquids can directly be delivered to tower, send into tower after also can converging with the liquid nitrogen of extracting out in condenser/evaporator (or liquid nitrogen fraction).
Described extra cold carrier also can be the cryogenic liquid that the liquefaction cycle equipment that added by above-mentioned air separation process provides.This cryogenic liquid is a liquid nitrogen, or liquid nitrogen fraction, or liquid air.
Described extra cold carrier also can be a part air of participating in rectifying through the last tower that removes rectifying column behind the booster expansion turbine that increases newly.This part air has also added cold to air-separating plant.
After the present invention adopts abovementioned technology, utilize cold energy of liquefied natural gas to come to have increased in the method for separation of air and add extra this method of cold carrier, can be when liquefied natural gas be under-supply, even there be not liquefied natural gas when supply, air-separating plant still can continue Steady and turn round surely, and the situation of frequent increasing and decreasing load and start-stop car can not take place.The cost of unit product still can descend significantly.
Description of drawings
Accompanying drawing 1 is the schematic diagram of embodiments of the invention 1.
Accompanying drawing 2 is the schematic diagram of embodiments of the invention 2.
Accompanying drawing 3 is the schematic diagram of embodiments of the invention 3.
Equipment serial number is as follows among the figure: 1 is main heat exchanger, and 2 is rectifying column, and 3 are following tower, 4 is last tower, 5 is condenser/evaporator, and 6 is liquid air subcooler, and 7 is liquid nitrogen subcooler, 8 is the nitrogen supercharging machine, 9 is nitrogen compressor, 10 and 10-1 be heat exchanger, 11 is the liquefied natural gas heat exchanger, 12 is gas-liquid separator, and 13 is liquefaction device.
Relevant material flow is also made following numbering: 101 are raw air, 102 is oxygen-enriched liquid air, 103 is returning polluted nitrogen, 104 is the nitrogen of drawing from following top of tower, 105 is the liquid nitrogen of drawing from condenser/evaporator 5,106 is the liquid oxygen product, 107 is the gas nitrogen of being drawn by gas-liquid separator, 108 are supercharging, cooled nitrogen, 109 is liquefied natural gas, and 110 is natural gas, and 111 for leaving the gas-liquid mixture of the nitrogen liquefied natural gas heat exchanger and after throttling, 112 for leaving the liquid nitrogen of gas-liquid separator, 113 is nitrogen products, and 114 is argon ` part, the 115 extraneous cryogenic liquids that directly provide into air separation unit of serving as reasons, 116 for being infeeded the cryogenic liquid of air separation unit by the liquefaction cycle of additional production cryogenic liquid, 118 is the nitrogen that the last top of tower of rectifying column.
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples.
Embodiment 1.As shown in Figure 1, through compressor compresses and cooling and in cleaning system, remove water vapour in chilldown system, raw air 101 behind the objectionable impurities such as carbon dioxide enters main heat exchanger 1, after cooling to Eat and temperature or partly being with liquid, enter the following tower 3 of rectifying column 2, rectifying column 2 is by following tower 3, and the condenser/evaporator 5 between last tower 4 and two towers is formed.Raw air 101 enters down the bottom of tower 3, becomes the ascending air of tower 3 down, falls the abundant contact of liquid stream in the column plate up and down and carries out the exchange of heat and quality.Bottom at following tower 3 obtains to contain the more oxygen-enriched liquid air of oxygen 102.After this oxygen-enriched liquid air 102 was drawn down tower 3, cold excessively by the returning polluted nitrogen 103 that is come by last tower 4 tops through liquid air subcooler 6 earlier, entering tower 4 through throttling expansion again became one of phegma of going up tower 4.The nitrogen that obtains at the following top of tower 3 is divided into two parts, and a part of nitrogen enters supercharger 8 after converging with another strand nitrogen 107 after the re-heat in heat exchanger 1.Be condensed into liquid nitrogen by liquid oxygen in the condenser/evaporator 5 of another part nitrogen between Liang Ta.The part of this liquid nitrogen becomes the phegma of tower 3 down, cold excessively by the returning polluted nitrogen 103 that is come by last tower 4 tops through liquid nitrogen subcooler 7 another part liquid nitrogen is drawn the back and converged from the liquid nitrogen 112 of gas-liquid separator 12 from condenser/evaporator 5 after, small part is as product 113 outer confessions; The top that the throttling expansion of most of process enters tower 4 becomes another strand phegma of going up tower 4.Above-mentioned two strands of phegmas become the decline liquid stream of going up tower 4.Decline liquid stream fully contacts the exchange of carrying out heat and quality with ascending air on column plate.Bottom at last tower 4 obtains liquid oxygen, small part can be used as product 106 outer confessions, be heated into gas oxygen by gas nitrogen in the condenser/evaporator 5 of most of liquid oxygen between Liang Ta, this gas oxygen becomes the ascending air of going up tower 4, also can extract small part as supplying outside product is after re-heat.Obtain returning polluted nitrogen 103 at the top of last tower 4, the re-heat in liquid nitrogen subcooler 7 and liquid air subcooler 6 of this portion gas enters the technology precalculated position after entering main heat exchanger 1 re-heat again.
The part nitrogen 104 of drawing by following tower 3 tops through main heat exchangers 1 re-heat after with converge from gas-liquid separator 12 and through the nitrogen 107 of re-heat, together enter 8 superchargings of nitrogen supercharging machine and heat exchanger 10 in, cool off; These nitrogen 108 enter liquefied natural gas heat exchanger 11 and liquefied natural gas 109 heat exchange and cooling subsequently, and liquefied natural gas 109 obtains leaving to use it for anything else after gasification and re-heat become natural gas 110 in liquefied natural gas heat exchanger 11.The gas-liquid mixture 111 that the nitrogen that leaves the liquefied natural gas heat exchanger carries out becoming after the throttling expansion nitrogen enters gas-liquid separator 12, the liquid nitrogen 112 that is flowed out by gas-liquid separator 12 converges with the liquid nitrogen 105 from condenser/evaporator 5, again through liquid nitrogen subcooler 7 cross cold after, a part can be used as product 113 outer confessions; The throttling expansion of most of process enters tower 4 as phegma.The gas nitrogen 107 that is obtained by gas-liquid separator 12 after the re-heat, converges with the nitrogen 104 of being drawn through main heat exchanger 1 by following tower 3 tops in liquefied natural gas heat exchanger 11, has finished nitrogen circulation.Containing the higher De Ya of argon Evaporated part 114 in the extraction of the appropriate location of last tower goes argon producing system to make the argon product.
When liquefied natural gas 109 supplys are not enough, can directly provide extra cryogenic liquid 115 by the external world to device.These extra cryogenic liquids 115 can directly be delivered to tower 4, send into tower 4 after also can converging with the liquid nitrogen of extracting out in condenser/evaporator (or liquid nitrogen fraction) 105.
Embodiment 2.Utilize technical process that the cold of liquefied natural gas comes separation of air as shown in Figure 2, the difference of present embodiment and embodiment 1 is: when liquefied natural gas 109 supplys were not enough, providing extra cryogenic liquid 116 to device was that the liquefaction device 13 that is added by air-separating plant provides.Top at last tower 4 obtains returning polluted nitrogen 103, the re-heat in liquid nitrogen subcooler 7 and liquid air subcooler 6 of this portion gas, a part enters the technology precalculated position after entering main heat exchanger 1 re-heat again, and another part enters liquefaction device 13, becomes extra cryogenic liquid 116 after treatment.
These extra cryogenic liquids 116 can directly be delivered to tower 4, send into tower 4 after also can converging with the liquid nitrogen of extracting out in condenser/evaporator (or liquid nitrogen fraction) 105.
Embodiment 3.Utilize technical process that the cold of liquefied natural gas comes separation of air as shown in Figure 3, the difference of present embodiment and embodiment 1 is: increased nitrogen compressor 9 newly, heat exchanger 10-1.The gas that enters nitrogen supercharging machine 8 is from three parts: a part is to leave following tower 3 tops of rectifying column 2 and the gas nitrogen after the re-heat in heat exchanger 1; A part be by gas-liquid separator 12 that obtain and in liquefied natural gas heat exchanger 11 the gas nitrogen 107 after the re-heat; A part is to leave re-heat in heat exchanger 1 behind last tower 4 tops of rectifying column 2, and the gas nitrogen that is compressed in nitrogen compressor 9 and cools off in heat exchanger 10-1.After this three parts gas nitrogen converges,, enter liquefied natural gas heat exchanger 11 and liquefied natural gas 109 heat exchange and cooling after the cooling of heat exchanger 10 through the supercharging of nitrogen supercharging machine 8.The gas-liquid mixture 111 that the nitrogen that leaves liquefied natural gas heat exchanger 11 carries out becoming after the throttling expansion nitrogen enters gas-liquid separator 12, and the gas nitrogen that is obtained by gas-liquid separator 12 enters nitrogen cycle again.Passage to air separation unit input cold carrier can be identical with embodiment 1 or embodiment 2.
Above-described only is preferred implementation of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the principle of the invention, can also make some modification and improvement, these also should be considered as belonging to protection scope of the present invention.
Claims (6)
1. air separating method that utilizes liquefied natural gas comprises:
(1) through compressor compresses and in chilldown system, cooling off, after in cleaning system, removing air (101) behind the impurity and in main heat exchanger (1), obtaining cold, enter the oxygen that rectifying column (2) is separated into various forms, nitrogen product and argon cut,
(2) drawing part gas nitrogen (104) by the top of following tower (3) joins with the gas nitrogen (107) from liquefied natural gas heat exchanger (11) after the re-heat in main heat exchanger (1), after supercharger (8) supercharging and heat exchanger (10) cooling, enter liquefied natural gas heat exchanger (11)
(3) after nitrogen (107) carries out the cold exchange after the nitrogen (108) that enters liquefied natural gas heat exchanger (11) and liquefied natural gas (109) throttling, in gas-liquid separator (12), be divided into the gentle nitrogen of liquid nitrogen (112) (107) through throttling expansion,
(4) liquid nitrogen (112) that obtains in gas-liquid separator (12) is joined with the liquid nitrogen (105) of being drawn by condenser/evaporator (5).Gas nitrogen (107) enters supercharger (8) after the re-heat with after above-mentioned gas nitrogen (104) junction in liquefied natural gas heat exchanger (11), finish nitrogen circulation,
It is characterized in that: in air separation process, add extra cold carrier.
2. the described a kind of air separating method that utilizes liquefied natural gas of root a tree name claim 1, it is characterized in that: described extra cold carrier is the cryogenic liquid that is directly provided by the external world.
3. the described a kind of air separating method that utilizes liquefied natural gas of root a tree name claim 1 is characterized in that: described extra cold carrier is the cryogenic liquid that the liquefaction cycle equipment (13) that added by above-mentioned air separation process provides.
4. root a tree name claim 2,3 described a kind of air separating methods that utilize liquefied natural gas, it is characterized in that: described cryogenic liquid is a liquid nitrogen, or liquid nitrogen fraction, or liquid air.
5. root a tree name claim 2,3 described a kind of air separating methods that utilize liquefied natural gas, it is characterized in that: cryogenic liquid can directly be delivered to tower (4), sends into tower (4) after also can converging with the liquid nitrogen of extracting out in condenser/evaporator (5) (or liquid nitrogen fraction) (105).
6. the described a kind of air separating method that utilizes liquefied natural gas of root a tree name claim 1 is characterized in that: described extra cold carrier is the part air through last tower (4) the participation rectifying of removing rectifying column (2) behind the booster expansion turbine that increases newly.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510022599 CN1789868A (en) | 2005-12-16 | 2005-12-16 | Air separating method by utilizing liquefied natural gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200510022599 CN1789868A (en) | 2005-12-16 | 2005-12-16 | Air separating method by utilizing liquefied natural gas |
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| CN1789868A true CN1789868A (en) | 2006-06-21 |
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| CN 200510022599 Pending CN1789868A (en) | 2005-12-16 | 2005-12-16 | Air separating method by utilizing liquefied natural gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101839612A (en) * | 2010-04-06 | 2010-09-22 | 浙江大学 | Backward flow type air separation system and method based on cold energy utilization of LNG (Liquefied Natural Gas) satellite station |
| 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 |
| WO2014114258A1 (en) * | 2013-01-27 | 2014-07-31 | 南京瑞柯徕姆环保科技有限公司 | Air separation apparatus for isobaric separation and production of oxygen and nitrogen |
-
2005
- 2005-12-16 CN CN 200510022599 patent/CN1789868A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101839612A (en) * | 2010-04-06 | 2010-09-22 | 浙江大学 | Backward flow type air separation system and method based on cold energy utilization of LNG (Liquefied Natural Gas) satellite station |
| 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 |
| WO2014114258A1 (en) * | 2013-01-27 | 2014-07-31 | 南京瑞柯徕姆环保科技有限公司 | Air separation apparatus for isobaric separation and production of oxygen and nitrogen |
| WO2014114138A1 (en) * | 2013-01-27 | 2014-07-31 | 南京瑞柯徕姆环保科技有限公司 | Air separation apparatus for isobaric separation and production of oxygen and nitrogen |
| CN103148676B (en) * | 2013-01-27 | 2016-03-30 | 南京瑞柯徕姆环保科技有限公司 | A kind of equipressure is separated the air separation unit producing oxygen nitrogen |
| US10060672B2 (en) | 2013-01-27 | 2018-08-28 | Nanjing Reclaimer Environmental Teknik Co., Ltd | Air separation apparatus to produce oxygen and nitrogen through isobaric separation |
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