CN100400995C - Method and device for air separation - Google Patents
Method and device for air separation Download PDFInfo
- Publication number
- CN100400995C CN100400995C CNB200610097738XA CN200610097738A CN100400995C CN 100400995 C CN100400995 C CN 100400995C CN B200610097738X A CNB200610097738X A CN B200610097738XA CN 200610097738 A CN200610097738 A CN 200610097738A CN 100400995 C CN100400995 C CN 100400995C
- Authority
- CN
- China
- Prior art keywords
- nitrogen
- heat exchanger
- main heat
- air
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
-
- 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
-
- 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
- F25J3/04357—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 and comprising a gas work expansion loop
-
- 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
-
- 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
-
- 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
-
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Air separation methods and devices, particularly relates to the air separation methods and devices when rectification is used in air separation at low temperatures. The pretreated raw air material is cooled at the main heat exchanger, directly enter into the rectifying column for rectification; compress and chill the returning polluted nitrogen (or returning nitrogen) leaving out the cooling box of the main heat exchanger, turbocharged and cooled, then enters the main heat exchanger and cooled to a certain temperature, the middle part was sent to polluted nitrogen (or nitrogen gas) expansion machine; gas works, reduces pressure and temperature then returned to the cooling heat exchanger, the remaining part was continually cooled in the main heat exchanger, after liquefied and cooled, join with part of the liquid nitrogen or polluted liquid nitrogen out of subcooler, after throttled and decompressed, get into the upper tower of the rectifying tower as the returning fluid of the tower, a gasometrical device was set on the pipeline of the returning polluted nitrogen (or returning nitrogen) cooling box; the air separation device can produce 10% more liquid nitrogen products and reduce the power consumption of products unit, further optimize performance cost proportion.
Description
Technical field
The present invention relates to a kind of method and apparatus of air separation, specially refer to the method and apparatus that utilizes rectifying to come separation of air at low temperatures.
Background technology
Before the present invention proposes, separate the single product that becomes various forms such as various components such as oxygen, nitrogen, argons with airborne, at first to adopt distillation technology to separate then air liquefaction.(critical-temperature is-140 because the condensing temperature of air is very low.7 ℃), come the method and apparatus of separation of air just to require the external world to provide lot of energy to obtain suitable cold with distillation technology at low temperatures.Especially when needs provide fluid product, the external world will provide more substantial energy.So the air separation industry is the industry of a high energy consumption.People have also proposed much to be intended to the air separating method and the device that cut down the consumption of energy.The Chinese patent notification number is the method and apparatus that the patent application case of CN1616909 has just proposed a kind of air separation.In air separation process, use the decompressor of swell refrigeration air and these two kinds of different working medium of returning polluted nitrogen (nitrogen reflux).Expand under each comfortable different pressure and temperature of swell refrigeration air and returning polluted nitrogen (nitrogen reflux), 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 more than the 0.65MPa (gauge pressure), and the operating pressure of last tower is more than the 0.08MPa (gauge pressure).Adopt such method and apparatus to come separation of air, the power consumption of unit product significantly decreases, and initial estimate can reduce by 10%.But, the liquid nitrogen that the condenser/evaporator that requires between two towers extracts, when increasing the liquid nitrogen product quantity of outwards supply, will correspondingly reduce as the amount of liquid nitrogen of last tower phegma.And when the liquid nitrogen of outer confession is increased to certain quantity, when promptly correspondingly reducing to certain quantity as the amount of liquid nitrogen of last tower phegma, the operating conditions of last tower will worsen, even influences the quality and quantity of rectifying column output object, do not reach user's demand, and make the economy variation.In some cases,, but in the air swell refrigeration process, have some unsatisfactory places, tend to cause the increase of power consumption even require the amount of liquid nitrogen of increase little.
Summary of the invention
The technical problem to be solved in the present invention is: overcome above-mentioned the deficiencies in the prior art, propose a kind of new air separating method and device, both can provide various morphological components products in normal scope; Can additionally increase the outer of liquid component product again, meet the need of market for quantity.Thereby further reduce power consumption, optimize the ratio of performance to price.
The present invention is achieved by the following technical solutions.The major technique feature of the method and apparatus of air separation is: through compressor compresses, cooling and in cleaning system, remove water vapour in chilldown system, air behind the objectionable impurities such as carbon dioxide through behind the main heat exchanger, directly enters rectifying column and carries out the rectifying operation; Simultaneously the returning polluted nitrogen (nitrogen reflux) that leaves main heat exchanger is compressed, be cooled to uniform temperature after, will be wherein a part send into dirty nitrogen (nitrogen) booster expansion turbine, gas externally does work, and returns heat exchanger as low-temperature receiver after the step-down cooling; Remaining part continues cooling in main heat exchanger, after the liquefaction (cold excessively in case of necessity), enter the phegma of the last tower of rectifying column as last tower through throttling.
On the pipeline of the returning polluted nitrogen that leaves the main heat exchanger cooling box (nitrogen reflux), be provided with tolerance and regulate facility;
On raw air and dirty nitrogen (nitrogen) pipeline, be provided with the low temperature of cold forecooler can be provided.
Pass through compressor compresses, in chilldown system, cool off and in cleaning system, remove water vapour, air behind the objectionable impurities such as carbon dioxide, cool to Eat and temperature or part with the following tower bottom that enters rectifying column behind the liquid through main heat exchanger, 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 nitrogen reflux) that is 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 outer confession after re-heat.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 (or nitrogen reflux) that is come by last top of tower through liquid nitrogen subcooler after remaining liquid nitrogen is drawn from condenser/evaporator, a part supplies outward as product; Remaining part and compressed, cooling, the liquid nitrogen fraction (or liquid nitrogen) of liquefaction after (cold excessively in case of necessity) converge another phegma of tower on the top that throttling expansion enters tower becomes.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, small part can be used as product and supplies outward, 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.The returning polluted nitrogen (or nitrogen reflux) that last top of tower obtains enters low pressure returning polluted nitrogen (or nitrogen reflux) decompressor after liquid nitrogen subcooler and liquid air subcooler re-heat, gas externally does work, and leaves main heat exchanger after returning the main heat exchanger re-heat after step-down is lowered the temperature.After returning polluted nitrogen (or nitrogen reflux) is compressed and is cooled to uniform temperature subsequently, interior in the dirty nitrogen of part (or nitrogen) enter dirty nitrogen (nitrogen) booster expansion turbine, gas externally does work, and returns heat exchanger as low-temperature receiver after the step-down cooling; Remaining part is further cooling liquefaction (cold excessively in case of necessity) and cross through throttling and to enter the phegma of the last tower of rectifying column as last tower after cold in main heat exchanger.The adding of this part phegma has improved the smart gold-plating operating mode of last tower, has guaranteed the technical-economic index of whole device.
In order to prevent the air-separating plant superpressure, on the pipeline of the returning polluted nitrogen (nitrogen reflux) of cooling box, be provided with tolerance and regulate facility.
Also the low temperature forecooler can be set, by the refrigeration unit in the external world, as freon refrigeration unit, ammonia refrigeration unit etc. provides cold to raw air and dirty nitrogen (nitrogen).
In the present invention, two dirty nitrogen (or nitrogen) decompressor is to start operation simultaneously.
In the present invention, two dirty nitrogen (or nitrogen vapour) decompressor is a booster expansion turbine.
Can extract out in the appropriate location of last tower and to contain the higher De Ya of argon Evaporated part and go argon producing system to make the argon product.
After the present invention adopted abovementioned technology, air-separating plant can be operated in normal range (NR); Also can be outside strengthening carry out operation under the situation of feed flow nitrogen product, Chu Bu Ce Suan can increase by 10% liquid nitrogen product amount.The power consumption of unit product can descend to some extent like this, and the ratio of performance to price is further optimized.
Description of drawings
Accompanying drawing 1,2 is respectively air separating method and the device schematic diagram of embodiment one, two.
Equipment serial number is as follows in interior: 1 is dirty nitrogen compressor, and 2 is water cooler, and 3 is the supercharger of dirty nitrogen booster expansion turbine, 4 is the water cooler behind the supercharger 3, and 5 is main heat exchanger, and 6 is the decompressor of dirty nitrogen booster expansion turbine, 7 is rectifying column, and 8 are following tower, and 9 is last tower, 10 is condenser/evaporator, and 11 is liquid air subcooler, and 12 is liquid nitrogen subcooler, 13 is the returning polluted nitrogen turbo-expander, 14 are tolerance adjusting facility, and 15 is the low temperature forecooler, and 16 is the cryogenic cooling unit.
Xiang Guan material flow is also made following numbering in addition: 101 are raw air, 102 is oxygen-enriched liquid air, 103 is returning polluted nitrogen, and 104 is the liquid oxygen product, and 105 is liquid nitrogen, 106 is liquid nitrogen product, 107 is the returning polluted nitrogen of return mechanism, and 108 is the argon cut, and 109 for removing the dirty nitrogen of swell refrigeration, 110 for removing the dirty nitrogen of tower after the liquefaction, 111 is the liquid nitrogen fraction of extracting out from following tower.
The specific embodiment
The invention will be further described below in conjunction with drawings and Examples.
Embodiment is just like shown in the accompanying drawing one, 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 used raw air as separating, after it cools to Eat and temperature or partly is with liquid through main heat exchanger 5, enter the following tower 8 of rectifying column 7, rectifying column 7 is by following tower 8, and the condenser/evaporator 10 between last tower 9 and two towers is formed.Raw air 101 becomes the ascending air of tower 8 down after entering down the bottom of tower 8, fall in the column plate up and down liquid stream fully contact carry out the exchange of heat and quality.Bottom at following tower 8 obtains to contain the more oxygen-enriched liquid air of oxygen 102.After this oxygen-enriched liquid air 102 was drawn down tower 8, cold excessively by the returning polluted nitrogen 103 that is come by last tower 9 tops through liquid air subcooler 11 earlier, entering tower 9 through throttling expansion again became one of phegma of going up tower 9.The nitrogen that obtains at the following top of tower 8, small part can be used as product outer confession after re-heat, in the condenser/evaporator 10 of most of nitrogen between Liang Ta and liquid oxygen heat exchange and be condensed into liquid nitrogen.Part liquid nitrogen becomes the phegma of tower 8 down.Remaining liquid nitrogen 105 is cold excessively by the returning polluted nitrogen 103 that is come by last tower 9 tops through liquid nitrogen subcooler 12, and a part is as product 106 outer confessions; The top that enters tower 9 through throttling expansion after remaining part and another strand liquid nitrogen fraction converge becomes another phegma of going up tower 9.Decline liquid stream fully contacts the exchange of carrying out heat and quality with ascending air on column plate.Bottom at last tower 9 obtains liquid oxygen, part liquid oxygen can be used as product 104 outer confessions, be heated into gas oxygen by nitrogen in the condenser/evaporator 10 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 9.The returning polluted nitrogen 103 that obtains at the top of last tower 9 enters returning polluted nitrogen turbo-expander 13 after the re-heat in liquid nitrogen subcooler 12 and liquid air subcooler 11, gas externally does work, and enters main heat exchanger 5 again after the step-down cooling.The returning polluted nitrogen 107 that leaves behind the main heat exchanger 5 is compressed in dirty nitrogen compressor 1, in water cooler 2, be cooled, supercharger 3 superchargings and the water cooler behind the supercharger 34 through dirty nitrogen booster expansion turbine cools off then, in main heat exchanger 5, be cooled again, the dirty nitrogen of part enters the decompressor 6 of dirty nitrogen booster expansion turbine in interior, gas externally does work, return main heat exchanger 5 as low-temperature receiver after the step-down cooling, remaining part further converges with the liquid nitrogen that goes out liquid nitrogen subcooler 12 after the cooling liquefaction in main heat exchanger 5, enters the phegma of the last tower 9 of rectifying column 7 as last tower 9 after the throttling step-down.Just can be increased to some extent by the quantity of the cold excessively outer feed flow nitrogen product 106 of the returning polluted nitrogen 103 that comes by last top of tower through liquid nitrogen subcooler 12 after drawing from condenser/evaporator 10 like this.
In order to prevent the air-separating plant superpressure, on the returning polluted nitrogen pipeline that leaves main heat exchanger 5 cooling box, be provided with by two adjustings and cut down the tolerance of being formed an adjusting facility 14.This adjusting facility 14 is used for controlling the tolerance of the returning polluted nitrogen 107 that enters dirty nitrogen compressor 1 and the tolerance of removing the returning polluted nitrogen in technology precalculated position.
Dirty nitrogen booster expansion turbine 3,6 and returning polluted nitrogen turbo-expander 13 are to start operation simultaneously.
Containing the higher De Ya of argon Evaporated part 108 in the extraction of the appropriate location of last tower goes argon producing system to make the argon product.
Embodiment two in air separating method identical with embodiment one and device, in order to reduce the energy consumption of product, is provided with low temperature forecooler 15 at the suitable position of main heat exchanger 5 shown in accompanying drawing two.And adopt cryogenic cooling unit 16 to separating with raw air 101 with through overcompression, water-cooled and the dirty nitrogen 107 of return mechanism provides cold.Simultaneously, Xia Ta top extract out liquid nitrogen fraction 111 cross through liquid nitrogen subcoolers 12 cold back and another strand liquid nitrogen fraction 110 converge tower 9 in the deutomerite diffluence as on the phegma of tower 9.The liquid nitrogen of extracting out in the condenser/evaporator 10 between Liang Ta 105 then all becomes liquid nitrogen product 106 after process liquid nitrogen subcooler 12 mistakes are cold.
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. the method for air separation comprises:
(1) through compressor compresses, the chilldown system cooling and in cleaning system, remove objectionable impurities after air (101) enter rectifying column (7) after through main heat exchanger (5), in rectifying column (7), be separated into the oxygen of various forms, nitrogen product and argon cut;
(2) enter returning polluted nitrogen or nitrogen reflux low-pressure expansion machine (13) after returning polluted nitrogen that obtains from the last tower (9) of rectifying column (7) or nitrogen reflux (103) re-heat, step-down laggard main heat exchanger (5) re-heat of going into of lowering the temperature in this low-pressure expansion machine (13);
It is characterized in that:
(1) directly enters rectifying column (7) behind air (101) the process main heat exchanger (5);
(2) leaving the returning polluted nitrogen of main heat exchanger (5) or nitrogen reflux (107) is compressed and cools off, after returning main heat exchanger (5) again, part enters dirty nitrogen or nitrogen high pressure expansion machine (6) in interior, gas externally does work, return main heat exchanger (5) after reducing pressure and reducing temperature, remaining part continues cooling in main heat exchanger (5), join with part liquid nitrogen that goes out liquid nitrogen subcooler (12) (105) or liquid nitrogen fraction (111), enters the last tower (9) of rectifying column (7) behind expenditure and pressure;
(3) returning polluted nitrogen or nitrogen reflux low-pressure expansion machine (13) and dirty nitrogen or nitrogen high pressure expansion machine (6) are to start operation simultaneously.
2. the device of air separation, successively by
(1) air is pressurizeed and remove compression, the chilldown system that objectionable impurities makes it to become raw air (101), and cleaning system,
(2) returning polluted nitrogen or nitrogen reflux (103) are carried out the low-pressure expansion machine (13) that step-down is lowered the temperature,
(3) various fluid is carried out the main heat exchanger (5) of cold and hot exchange, liquid air subcooler (11) and liquid nitrogen subcooler (12),
(4) will separate the rectifying column (7) that carries out separating obtained product with raw air, form,
It is characterized in that: also have
(1) dirty nitrogen or the nitrogen compressor (1) that the returning polluted nitrogen or the nitrogen reflux (107) of return mechanism compressed and cool off, water cooler (2), the supercharger (3) of high pressure booster expansion machine (6), the water cooler (4) behind the supercharger (3),
(2) will carry out the high pressure booster expansion turbine (6) of step-down cooling through overcompression, supercharging, cooled dirty nitrogen or nitrogen,
(3) on the pipeline of returning polluted nitrogen that leaves main heat exchanger (5) or nitrogen reflux, be provided with tolerance and regulate facility (14);
Main heat exchanger (5) links to each other with the following tower (8) of rectifying column (7) by pipeline, and the following tower (8) of rectifying column (7) is by the last tower of pipeline and liquid air subcooler (11), liquid nitrogen subcooler (12), rectifying column (7)
(9) link to each other; Last tower (9) links to each other with liquid nitrogen subcooler (12), liquid air subcooler (11), returning polluted nitrogen or nitrogen reflux low-pressure expansion machine (13) successively by pipeline, and then by tolerance regulate facility (14) successively with dirty nitrogen or nitrogen compressor (1), water cooler (2), the supercharger (3) of high pressure booster expansion turbine (6), the water cooler (4) behind the supercharger (3) links to each other;
Afterwards, by the water cooler (4) of pipeline after with supercharger (3) successively with main heat exchanger (5), high pressure booster expansion turbine (6), returning polluted nitrogen or nitrogen reflux low-pressure expansion machine (13) link to each other; Simultaneously by the water cooler (4) of pipeline after with supercharger (3) successively with main heat exchanger (5), the described tower (9) of going up of rectifying column (7) links to each other.
3. the device of air separation according to claim 2, it is characterized in that: returning polluted nitrogen or nitrogen reflux low-pressure expansion machine (13) are booster expansion turbines.
4. the device of air separation according to claim 2 is characterized in that: described tolerance is regulated facility (14) and is made of control valve.
5. the device of air separation according to claim 2 is characterized in that: be provided with the low temperature forecooler (15) of obtaining cold from the external world.
6. the device of air separation according to claim 5, it is characterized in that: providing the refrigeration unit of cold to low temperature forecooler (15) is low temperature refrigerator group (16).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610097738XA CN100400995C (en) | 2006-11-22 | 2006-11-22 | Method and device for air separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610097738XA CN100400995C (en) | 2006-11-22 | 2006-11-22 | Method and device for air separation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1975302A CN1975302A (en) | 2007-06-06 |
| CN100400995C true CN100400995C (en) | 2008-07-09 |
Family
ID=38125544
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200610097738XA Active CN100400995C (en) | 2006-11-22 | 2006-11-22 | Method and device for air separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100400995C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101943513B (en) * | 2010-09-30 | 2013-01-30 | 杭州川空通用设备有限公司 | Method for lowering liquid space division energy consumption |
| CN102564065A (en) * | 2012-01-15 | 2012-07-11 | 罗良宜 | Energy saving air liquefaction separation device |
| CN105758121A (en) * | 2014-12-19 | 2016-07-13 | 常熟市永安工业气体制造有限公司 | Pure nitrogen preparation device |
| 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 |
| CN114216301B (en) * | 2021-11-08 | 2023-04-25 | 常州市长宇实用气体有限公司 | Device and method for cryogenic separation and production of high-purity liquid nitrogen |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1152108A (en) * | 1995-11-07 | 1997-06-18 | 波克股份有限公司 | Air separation method and apparatus for producing nitrogen |
| JPH11142054A (en) * | 1997-11-04 | 1999-05-28 | Nippon Sanso Kk | Method and system for air liquefaction separation utilizing cold heat of liquefied natural gas |
| EP1058074A1 (en) * | 1999-06-04 | 2000-12-06 | Air Products And Chemicals, Inc. | Air separation process with a combustion engine for the production of atmospheric gas products and electric power |
| JP2001141359A (en) * | 1999-11-17 | 2001-05-25 | Toshiba Corp | Air separator |
| CN1616908A (en) * | 2004-10-28 | 2005-05-18 | 苏州市兴鲁空分设备科技发展有限公司 | Method and device for separating air |
-
2006
- 2006-11-22 CN CNB200610097738XA patent/CN100400995C/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1152108A (en) * | 1995-11-07 | 1997-06-18 | 波克股份有限公司 | Air separation method and apparatus for producing nitrogen |
| JPH11142054A (en) * | 1997-11-04 | 1999-05-28 | Nippon Sanso Kk | Method and system for air liquefaction separation utilizing cold heat of liquefied natural gas |
| EP1058074A1 (en) * | 1999-06-04 | 2000-12-06 | Air Products And Chemicals, Inc. | Air separation process with a combustion engine for the production of atmospheric gas products and electric power |
| JP2001141359A (en) * | 1999-11-17 | 2001-05-25 | Toshiba Corp | Air separator |
| CN1616908A (en) * | 2004-10-28 | 2005-05-18 | 苏州市兴鲁空分设备科技发展有限公司 | Method and device for separating air |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1975302A (en) | 2007-06-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101886871B (en) | Method and device for producing pressure oxygen by air separation | |
| CN100472159C (en) | Air separating device and method therefor | |
| CN204115392U (en) | With the full air separation units producing liquids of air supply compressor | |
| CN104807286A (en) | Nitrogen liquefaction system allowing recycling of LNG (Liquefied Natural Gas) cold energy | |
| CN100400995C (en) | Method and device for air separation | |
| CN104061756B (en) | Returning polluted nitrogen gas demi-inflation refrigeration and partial boost enter pressure column and to be coupled the method and device of producing nitrogen under pressure product | |
| CN2811892Y (en) | Air separator by back streaming expansion | |
| CN104755360A (en) | Method and apparatus for air separation by cryogenic distillation | |
| CN105066587A (en) | Cryogenic separation and low-purity oxygen and high-purity oxygen and nitrogen production device and method | |
| CN101915495B (en) | Full liquid-air separation unit using liquefied natural gas cold energy and method thereof | |
| CN202204239U (en) | Device for producing high-purity nitrogen and low-purity oxygen with pressure | |
| CN109883139B (en) | Efficient argon extraction process based on oxygen-enriched air separation | |
| CN103759500A (en) | Method and device for manufacturing high purity nitrogen in low energy consumption mode | |
| CN109323533B (en) | Method and device for reducing space division energy consumption by using medium-pressure rectifying tower | |
| CA2634483A1 (en) | Cryogenic air separation system | |
| CN102032756A (en) | Air separation method | |
| CN100443838C (en) | Method and equipment for separating stream backed expansion air | |
| CN102530892A (en) | Method for producing high purity nitrogen and under-pressure low purity oxygen | |
| CN204718303U (en) | A kind of air-separating plant preparing pressure oxygen | |
| CN1038514A (en) | Produce the air separating technological of hyperbaric oxygen and elevated pressure nitrogen | |
| CN203687518U (en) | Low-purity oxygen preparing device with auxiliary rectifying tower | |
| CN102141337A (en) | Method for separating air | |
| CN100357684C (en) | Method and device for separating air | |
| CN201876055U (en) | Full-liquid air separation device using cold energy of liquefied natural gas | |
| CN102052821A (en) | Air separation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |