CN1687678A - Method and equipment for separating stream backed expansion air - Google Patents
Method and equipment for separating stream backed expansion air Download PDFInfo
- Publication number
- CN1687678A CN1687678A CN 200510039072 CN200510039072A CN1687678A CN 1687678 A CN1687678 A CN 1687678A CN 200510039072 CN200510039072 CN 200510039072 CN 200510039072 A CN200510039072 A CN 200510039072A CN 1687678 A CN1687678 A CN 1687678A
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- nitrogen
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- air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04309—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 nitrogen
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen 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
- F25J3/04248—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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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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 is the backflow expansion air separating method and the equipment, and relates to the method and equipment that use rectification and backflow expansion to separate the air. During the air separation process, the invention uses the product nitrogen and the dirt nitrogen expansion machines. The product nitrogen and the dirt nitrogen expanse separately under different conditions and provide the cold power for the air separation. The separation process adopts the double-grade rectification tower that is composed of the lower tower, the upper tower and the chill evaporator between the two towers. The operational pressure of the lower tower is above 0.65MPa and the upper tower is above 0.08MPa. The invention greatly reduces the cost and optimizes the ratio of performance to price.
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 and stream backed expansion to come separation of air at low temperatures.
Background technology
Before the present invention proposed, utilizing rectifying to come separation of air at low temperatures was a kind of known industrial production technology.Usual way is: the air of process compressor compresses cools off in chilldown system and remove water vapour in cleaning system, is divided into two strands of air-flows behind the objectionable impurities such as carbon dioxide.One air-flow is that swell refrigeration flows with air, enter heat exchanger after its process supercharger supercharging and the water cooler cooling, enter decompressor after the reduction temperature, air externally does work, after the step-down cooling, send into again and get back to the import of compressor or remove water-cooling tower after tower participates in rectifying or returns the heat exchanger re-heat.Another strand air-flow is for separating with air stream, and it cools to Eat and temperature or part with the bottom that enters tower under the rectifying column behind the liquid through heat exchanger.Rectifying column generally by following tower, form by 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 enters Shang Ta through cold excessively and throttling expansion after being drawn down tower, as the phegma of last tower.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 down tower, 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, a part of liquid oxygen can be used as product and draws, most liquid oxygen is heated as gas oxygen by nitrogen in condenser/evaporator, a part of gas oxygen also can be used as product outer confession after re-heat, and most gas oxygen is then as ascending air participation rectifying.The top of last tower can obtain nitrogen and dirty nitrogen.Suitable position at last tower can also extracting go out to contain the higher fraction of argon, can obtain the product argon at argon producing system by rectifying.Adopt such method and apparatus to come separation of air to obtain the oxygen of different shape, nitrogen and argon, particularly liquid oxygen, nitrogen product and (or) pressure oxygen, nitrogen product, the power consumption of unit product is higher.
Summary of the invention
The objective of the invention is to propose the method and apparatus of air separation under a kind of new low temperature, make the bigger decline of power consumption of unit product.The ratio of performance to price of device is better.Working service is also easier.
The present invention is achieved by the following technical measures.Major technique feature of the present invention is: in the process of air separation, used the decompressor of these two kinds of different working medium of product nitrogen and returning polluted nitrogen.Expand under each comfortable different temperature of product nitrogen and returning polluted nitrogen, outwards acting is for air separation process provides cold.Double rectification column is adopted in separation process, and rectifying column is by following tower, and the condenser/evaporator between Shang Ta and two towers is formed.The operating pressure of following tower is that the operating pressure of last tower is more than the 0.08MPa more than the 0.65MPa (gauge pressure, down together).And a kind of in product nitrogen decompressor and the returning polluted nitrogen decompressor be booster expansion turbine, and another kind of decompressor then can be with also can not be with supercharger.
In chilldown system, cool off and in cleaning system, remove water vapour through the air of compressor compresses, objectionable impurities such as carbon dioxide is gone into main heat exchanger after supercharger supercharging of overexpansion machine and water cooler cooling are laggard, through cooling to after Eat and temperature or part enter the following tower bottom of rectifying column after with liquid with the gas converting heat that backflows, 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 and the product nitrogen of being come by last top of tower through liquid air subcooler earlier, entering Shang Ta through throttling expansion again became one of phegma of going up tower.The nitrogen that obtains at the following top of tower, small part can be used as product after re-heat outside confession, be condensed into liquid nitrogen with the liquid oxygen heat exchange in the condenser/evaporator of most of nitrogen between Liang Ta.The part of this liquid nitrogen becomes the phegma of tower down.Cold excessively by the returning polluted nitrogen and the product nitrogen of being come by last top of tower through liquid nitrogen subcooler after remaining liquid nitrogen is drawn from condenser/evaporator, small part supplies outward as product; The top that the throttling expansion of most of process enters tower becomes another 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, a part can be used as product and supplies outward, a part goes to use a little after the re-heat in the hot device of Zai Zai Change after cryogenic liquid pump boosts, be heated into gas oxygen by nitrogen in the condenser/evaporator of most of liquid oxygen between Liang Ta, small part gas oxygen can be used as product after re-heat outside confession, remaining gas oxygen becomes the ascending air of going up tower.Returning polluted nitrogen and product nitrogen that last top of tower obtains enter returning polluted nitrogen decompressor and product nitrogen decompressor respectively, and gas externally does work, and enter the technology precalculated position after returning the heat exchanger re-heat after the step-down cooling.
In the present invention, the returning polluted nitrogen that obtains at the top of last tower and the temperature of product nitrogen are lower, can be at liquid nitrogen subcooler, and cold section re-heat of liquid air subcooler and main heat exchanger.Therefore in returning polluted nitrogen decompressor and the product nitrogen decompressor can be positioned at before the liquid nitrogen subcooler; Or be positioned in the middle of liquid nitrogen subcooler and the liquid air subcooler; Or be positioned at after the liquid air subcooler.Another then is positioned at a certain position of cold section of main heat exchanger.
In the present invention, product nitrogen decompressor and returning polluted nitrogen decompressor are to start operation simultaneously.
In the present invention, one in returning polluted nitrogen decompressor and the product nitrogen decompressor is booster expansion turbine, and another kind of decompressor then can be with also can not be with supercharger.
In the present invention, can contain the higher De Ya of argon Evaporated part in the extraction of the appropriate location of last tower goes argon producing system to make the argon product.
In the present invention, high pressure heat exchanger and cryogenic pump are set also, when supplying the small amount of liquid product outside, supply interior compressed product gas outward.
After the invention process abovementioned technology, apparatus cost is declined to a great extent, the more similar flow process of the power consumption of unit product significantly decreases, and can optimize the ratio of performance to price, uses and keeps in repair more convenient and economical.
Description of drawings
Accompanying drawing is stream backed expansion air separating method and device schematic diagram.Equipment serial number is as follows in interior: 1 is the decompressor supercharger, and 2 is water cooler, and 3 is main heat exchanger, and 4 is dirty nitrogen decompressor, 5 is rectifying column, and 6 are following tower, and 7 is last tower, and 8 is condenser/evaporator, 9 is liquid air subcooler, and 10 is liquid nitrogen subcooler, and 11 is the product nitrogen decompressor, and 12 is cryogenic liquid pump.Xiang Guan material flow is also made following numbering in addition: 101 are raw air, and 104 is oxygen-enriched liquid air, and 105 is product nitrogen, and 106 is liquid oxygen, 107 is liquid nitrogen, and 108 is liquid nitrogen product, and 109 is the argon cut, 110 is returning polluted nitrogen, and 111 is the liquid oxygen product, and 112 is interior compressed oxygen product.
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples.
The cooling in chilldown system of process compressor compresses is also removed water vapour in cleaning system, raw air 101 behind the objectionable impurities such as carbon dioxide is gone into main heat exchanger 3 through decompressor supercharger 1 superchargings and water cooler 2 coolings are laggard, after process main heat exchanger 3 cools to Eat and temperature or partly is with liquid, enter the following tower 6 of rectifying column 5, rectifying column 5 is by following tower 6, and the condenser/evaporator 8 between last tower 7 and two towers is formed.The operating pressure of following tower 6 is 0.65Mpa, and the operating pressure of last tower 7 is 0.08MPa.Separation enters down the bottom of tower 6 with raw air stream 101, becomes the ascending air of tower 6 down, falls liquid stream in the column plate up and down and fully contacts and carry out the exchange of heat and quality.Bottom at following tower 6 obtains to contain the more oxygen-enriched liquid air of oxygen 104.After this oxygen-enriched liquid air 104 was drawn down tower 6, cold excessively by the product nitrogen 105 and the returning polluted nitrogen 110 that are come by last tower 7 tops through liquid air subcooler 9 earlier, entering tower 7 through throttling expansion again became one of phegma of going up tower 7.The nitrogen that obtains at the following top of tower 6, small part can be used as product outer confession after re-heat, in the condenser/evaporator 8 of most of nitrogen between Liang Ta and liquid oxygen heat exchange and be condensed into liquid nitrogen.The part of this liquid nitrogen becomes the phegma of tower 6 down.Remaining liquid nitrogen 107 is cold excessively by the product nitrogen 105 and the returning polluted nitrogen 110 that are come by last tower 7 tops through liquid nitrogen subcooler 10, and small part is as product 108 outer confessions; The top that the throttling expansion of most of process enters tower 7 becomes another phegma of going up tower 7.Above-mentioned two strands of phegmas become the decline liquid stream of going up tower 7.Decline liquid stream fully contacts the exchange of carrying out heat and quality with ascending air on column plate.Bottom at last tower 7 obtains liquid oxygen, part liquid oxygen can be used as product 111 outer confessions, a part liquid oxygen through cryogenic liquid pump 12 boost to required pressure after main heat exchanger 3 re-heats, become in compressed oxygen product 112 go to use a little, be heated into gas oxygen by nitrogen in the condenser/evaporator 8 of all the other liquid oxygen between Liang Ta, small part gas oxygen can be used as product after re-heat outside confession, its residual air oxygen becomes the ascending air of going up tower 7.The product nitrogen 105 that obtains at the top of last tower 7 enters product nitrogen decompressor 11 after the re-heat in liquid nitrogen subcooler 10 and liquid air subcooler 9, gas externally does work, enter liquid air subcooler 9 and main heat exchanger 3 re-heats again after the step-down cooling, draw ice chest afterwards as product.The returning polluted nitrogen 110 that obtains on the top of last tower 7 removes returning polluted nitrogen decompressor 4 at liquid nitrogen subcooler 10 after 3 cold sections re-heats of liquid air subcooler 9 and main heat exchanger, and the step-down cooling is laggard goes into main heat exchanger 3 and raw air heat exchange, goes to the technology precalculated position afterwards.Two decompressors 4 and 11 position on stream can Hu Change.Returning polluted nitrogen decompressor 4 and product nitrogen decompressor 11 are to start operation simultaneously.
Containing the higher De Ya of argon Evaporated part 109 in the extraction of the appropriate location of last tower goes argon producing system to make the argon product.
The present invention is not limited to above-mentioned embodiment; no matter on its method or device, do any variation; all decompressors with these two kinds of different working medium of product nitrogen gas and returning polluted nitrogen; and the operating pressure of following tower is more than the 0.65MPa (gauge pressure), and the operating pressure of last tower is that above twin-stage rectifying air separating method of 0.08MPa (gauge pressure) and device all drop within protection scope of the present invention.
Claims (7)
1. the method for a stream backed expansion air separation, comprise: through compressor compresses, chilldown system cooling and in cleaning system, remove objectionable impurities after supercharger (1) supercharging that drives via decompressor of air (101) after in main heat exchanger (3), be cooled to enter rectifying column (5) behind the part band liquid, in rectifying column (5), be separated into the oxygen of various forms, nitrogen product and argon cut
It is characterized in that:
(1) enters product nitrogen decompressor (11) after the product nitrogen gas (105) of drawing from last tower (7) passes through liquid nitrogen subcooler (10) and liquid air subcooler (9) re-heat, send into main heat exchanger (3) after subcooler (9) is returned in step-down cooling back in product nitrogen decompressor (11), going out main heat exchanger (3) back exports as product
(2) returning polluted nitrogen (110) that obtains from the last tower (7) of rectifying column (5) through liquid nitrogen subcooler (10) and liquid air subcooler (9) after, enter enter returning polluted nitrogen decompressor (4) step-down cooling after cold section preliminary re-heat of main heat exchanger (3) after, go to the technology precalculated position after entering main heat exchanger (3) re-heat again
(3) returning polluted nitrogen decompressor (4) and product nitrogen decompressor (11) are to start operation simultaneously,
(4) operating pressure of the following tower (6) of rectifying column (5) is more than the 0.65MPa (gauge pressure), and upward the operating pressure of tower (7) is more than the 0.08MPa (gauge pressure).
2. the method for a kind of stream backed expansion air separation according to claim 1 is characterized in that: the product nitrogen (105) that obtains from the last tower (7) of rectifying column (5) enters product nitrogen decompressor (11) before entering liquid nitrogen subcooler (10).
3. the method for a kind of stream backed expansion air separation according to claim 1 is characterized in that: go into product nitrogen decompressor (11) from the product nitrogen (105) that the last tower (7) of rectifying column (5) obtains afterwards through liquid nitrogen subcooler (10).
4. the method for a kind of stream backed expansion air separation according to claim 1 is characterized in that: product nitrogen decompressor (11) and returning polluted nitrogen decompressor (4) position on stream can exchange.
5. the device of a stream backed expansion air separation, successively by
(1) air is pressurizeed and remove the compressor that objectionable impurities makes it to become raw air, chilldown system, and cleaning system,
(2) raw air is carried out the decompressor supercharger (1) of supercharging and cooling, water cooler (2),
(3) various fluid is carried out the main heat exchanger (3) of cold and hot exchange, subcooler (9) and (10),
(4) will separate rectifying column (5) composition that carries out separating obtained product with raw air,
It is characterized in that:
(1) also have the product nitrogen decompressor (11) that product nitrogen is carried out the step-down cooling, and returning polluted nitrogen carried out the returning polluted nitrogen decompressor (4) that step-down is lowered the temperature,
(2) rectifying column (5) is a double rectification column, is the above following tower (6) of 0.65MPa (gauge pressure) by operating pressure, and operating pressure is that above last tower (7) of 0.08MPa (gauge pressure) and the condenser/evaporator (8) between two towers are formed.
6. a kind of stream backed expansion air-separating plant according to claim 5 is characterized in that: returning polluted nitrogen decompressor (4) is a booster expansion turbine, and product nitrogen decompressor (11) can be with also can not be with supercharger.
7. the device of a kind of stream backed expansion air separation according to claim 5 is characterized in that: product nitrogen decompressor (11) is a booster expansion turbine, and returning polluted nitrogen decompressor (4) can be with also can not be with supercharger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100390728A CN100443838C (en) | 2005-04-20 | 2005-04-20 | Method and equipment for separating stream backed expansion air |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100390728A CN100443838C (en) | 2005-04-20 | 2005-04-20 | Method and equipment for separating stream backed expansion air |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1687678A true CN1687678A (en) | 2005-10-26 |
| CN100443838C CN100443838C (en) | 2008-12-17 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100390728A Active CN100443838C (en) | 2005-04-20 | 2005-04-20 | Method and equipment for separating stream backed expansion air |
Country Status (1)
| Country | Link |
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| CN (1) | CN100443838C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104061756A (en) * | 2014-06-09 | 2014-09-24 | 杭州杭氧股份有限公司 | Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting |
| CN106196886A (en) * | 2016-07-13 | 2016-12-07 | 浙江智海化工设备工程有限公司 | In a kind of Novel low-consumption oxygen, compressed nitrogen expands the space division flow process without air expander |
| 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 |
| CN109059422A (en) * | 2018-07-12 | 2018-12-21 | 北京拓首能源科技股份有限公司 | A kind of device using dirty nitrogen cold energy precooled air |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0721378B2 (en) * | 1985-08-12 | 1995-03-08 | 大同ほくさん株式会社 | Oxygen gas production equipment |
| FR2709538B1 (en) * | 1993-09-01 | 1995-10-06 | Air Liquide | Method and installation for producing at least one pressurized air gas. |
| US5582034A (en) * | 1995-11-07 | 1996-12-10 | The Boc Group, Inc. | Air separation method and apparatus for producing nitrogen |
| JP2875206B2 (en) * | 1996-05-29 | 1999-03-31 | 日本エア・リキード株式会社 | High purity nitrogen production apparatus and method |
| JP3748677B2 (en) * | 1997-08-13 | 2006-02-22 | 大陽日酸株式会社 | Method and apparatus for producing low purity oxygen |
| US5966967A (en) * | 1998-01-22 | 1999-10-19 | Air Products And Chemicals, Inc. | Efficient process to produce oxygen |
-
2005
- 2005-04-20 CN CNB2005100390728A patent/CN100443838C/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104061756A (en) * | 2014-06-09 | 2014-09-24 | 杭州杭氧股份有限公司 | Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting |
| CN106196886A (en) * | 2016-07-13 | 2016-12-07 | 浙江智海化工设备工程有限公司 | In a kind of Novel low-consumption oxygen, compressed nitrogen expands the space division flow process without air expander |
| 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 |
| CN109059422A (en) * | 2018-07-12 | 2018-12-21 | 北京拓首能源科技股份有限公司 | A kind of device using dirty nitrogen cold energy precooled air |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100443838C (en) | 2008-12-17 |
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