CN103277981B - Device and method for increasing nitrogen-to-oxygen ratio of air separation unit - Google Patents
Device and method for increasing nitrogen-to-oxygen ratio of air separation unit Download PDFInfo
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- CN103277981B CN103277981B CN201310237929.1A CN201310237929A CN103277981B CN 103277981 B CN103277981 B CN 103277981B CN 201310237929 A CN201310237929 A CN 201310237929A CN 103277981 B CN103277981 B CN 103277981B
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- nitrogen
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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
- F25J3/04406—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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
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- 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
The invention relates to a device and a method for increasing the nitrogen-to-oxygen ratio of an air separation unit. On the basis of an existing air separation unit, and on the condition of not increasing energy consumption basically, the nitrogen-to-oxygen ratio of the air separation unit is increased to 2:1 or meets the requirement on continually increasing demand ratio of nitrogen and oxygen of users. The device comprises a main heat exchanger, an expansion machine, a sub-cooler, a main rectifying column and an ice chest. The main rectifying column is provided with a lower column, an evaporator condenser and an upper column. An auxiliary column is omitted, and meanwhile, the upper column is heightened by about 30% on the basis of the original height. The upper column is directly connected with a nitrogen pipeline. Nitrogen and waste nitrogen are delivered by the aid of an original waste nitrogen pipeline and the nitrogen pipeline respectively, and are discharged from the ice chest to be fed into respective pipelines after heat exchange. Cost required for pipeline and heat-exchange equipment modification is saved.
Description
Technical field
The present invention relates to a kind of device and method improving air separation unit nitrogen oxygen product ratio.
Background technology
In recent years, along with the maximization of blast furnace in metallurgical industry, converter and applying of oxygen-rich smelting technology, the demand percentage of smelter to oxygen, nitrogen there occurs larger change, main manifestations is be greater than growth to oxygen demand to the growth of nitrogen demand, according to rough Statistics, nitrogen oxygen has original 1:1 than demand, has brought up to 1.2:1 or higher.But first wife overlaps oxygen producing, air separation unit nitrogen oxygen product ratio when designing of nitrogen is generally 1:1, and the output of oxygen, nitrogen product does not have large change substantially after putting into operation.If the oxygen generating plant that newly-built nitrogen oxygen product ratio is greater than 1:1 substitutes existing equipment, so existing equipment is idle causes waste; If according to the newly-built equipment of making nitrogen of nitrogen breach, the significantly raising of production cost so certainly will to be caused.And there is no effective reforming mode at present, to meet the change of current oxygen nitrogen than demand.
As everyone knows, atmospheric oxygen content (on volume) accounts for 20.9%, and nitrogen content (on volume) accounts for 78.1%.When air separation unit nitrogen oxygen product ratio is 1:1, dirty nitrogen output is then 57.2%, for 2 times of nitrogen output also want many, this is with regard to for transforming existing air separation unit equipment component, and the exchange of nitrogen, dirty stream of nitrogen gas passage provides condition to improve nitrogen oxygen product ratio.
Summary of the invention
Object of the present invention effectively cannot meet oxygen nitrogen than change for solving existing air separation unit exactly, and lack the problem of effective reforming mode, a kind of device and method improving air separation unit nitrogen oxygen product ratio is provided, it is on existing air separation unit basis, and when substantially not increasing energy consumption, meet user to the ever-increasing demand of nitrogen oxygen product demand percentage.
For achieving the above object, the present invention adopts following technical scheme:
A kind of device improving air separation unit nitrogen oxygen product ratio, comprise main heat exchanger, decompressor, subcooler, main distillation column, ice chest, described main distillation column is only provided with lower tower, condenser/evaporator, upper tower, make while cancelling auxiliary tower the basis of tower tower height degree on former increases about 30%, upper tower is directly connected with nitrogen pipeline, nitrogen in ice chest, dirty stream of nitrogen gas passage is carrying out mutual switching with upper tower junction, namely nitrogen utilizes former dirty nitrogen pipeline to carry out heat exchange and conveying, dirty nitrogen then utilizes former nitrogen pipeline to carry out heat exchange and conveying, nitrogen, former pipeline is switched to again after dirty nitrogen cooling box.
A compressed-air actuated part through purifying through decompressor pressuring expansion, then after main heat exchanger, subcooler cooling, enters tower on main fractionating tower and participates in rectifying, and another part directly enters tower under main fractionating tower through main heat exchanger and participates in rectifying; Lower tower bottom liquid air enters in the middle part of upper tower through subcooler and participates in rectifying, and lower top of tower nitrogen enters the condenser/evaporator post liquefaction of main distillation column, and a part is back to lower tower, and another part enters upper top of tower through subcooler and participates in rectifying, and fixed gas is directly emptying; Oxygen cooling box after subcooler, main heat exchanger re-heat that upper tower bottom is extracted out, dirty nitrogen is still taken out by upper tower middle and upper part, but gas channel and stream of nitrogen gas passage switch in ice chest, the former dirty nitrogen pipeline of access is switched after subcooler, main heat exchanger cooling box, the top that the upper tower increased when nitrogen is then constant by the equivalent number of plates substitutes original auxiliary tower is taken out, in ice chest, gas channel correspondingly switches with dirty stream of nitrogen gas passage, switches the former nitrogen pipeline of access after subcooler, main heat exchanger cooling box.
Adopt a method for the raising nitrogen oxygen product ratio improving air separation unit nitrogen oxygen product proportioning device, make while cancelling auxiliary tower the basis of tower tower height degree on former increases about 30%, make tower nitrogen withdrawal amount bring up to original more than 2 times, the actual conditions that after increasing according to nitrogen withdrawal amount, dirty nitrogen amount declines, by nitrogen, dirty nitrogen carries out the mutual switching of gas channel from taking-up place of upper tower, namely nitrogen utilizes former dirty nitrogen pipeline to carry out heat exchange and conveying, dirty nitrogen then utilizes former nitrogen pipeline to carry out heat exchange and conveying, both existing pipeline and heat transmission equipment had been taken full advantage of, again save because nitrogen withdrawal amount increases rear pipeline modification, the expense caused is changed in subcooler and the change of main heat exchanger heat exchange area to be increased, and after cooling box, correspondingly switch to former pipeline, make the nitrogen oxygen product ratio of whole air separation unit by 1:1 brought up to 2:1 and more than.
The invention has the beneficial effects as follows: under the condition substantially not increasing operating cost, by tower on air separation unit increase transformation with nitrogen, dirty stream of nitrogen gas passage mutual switching, achieve air separation unit nitrogen oxygen product ratio by 1:1 bring up to 2:1 and more than, saved the newly-built air separation unit occupation of capital and used equipment and to have left unused the waste caused.Such as 20000Nm
3after/h grade air separation unit improves nitrogen oxygen product ratio, nitrogen output is by 20000Nm
3/ h brings up to 60000Nm
3/ h, by confessing profit 0.01 yuan/m
3calculate, can increase profit the whole year is: (60000-20000) × 365 × 24 × 0.01=350.4 ten thousand yuan.
Accompanying drawing explanation
Fig. 1 existing air separation unit oxygen-nitrogen production technological process;
Fig. 2 air separation unit oxygen-nitrogen of the present invention production technological process;
In figure, 1. booster expansion turbine group, 2. ice chest, 3. main heat exchanger, 4. subcoolers, 5. descend tower, 6. main distillation column, 7. condenser/evaporator, 8. go up tower, 9. auxiliary tower, 10. channel of nitrogen, 11. dirty channel of nitrogen.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention will be further described:
In Fig. 1, a compressed air part through purification enters ice chest 2 after booster expansion turbine group 1 supercharging, to expand cooling through booster expansion turbine group 1 after main heat exchanger 3 tentatively cooling, the middle and upper part directly sending into the upper tower 8 (upper tower 8 tower height degree basis increases 30% on former) of main distillation column 6 after main heat exchanger 3, subcooler 4 are lowered the temperature participates in rectifying again; The lower tower 5 that another part directly sends into main distillation column 6 after main heat exchanger 3 is lowered the temperature participates in rectifying.The liquid air that lower tower bottom takes out enters in the middle part of upper tower 8 and participates in rectifying after subcooler 4 is excessively cold; The condenser/evaporator 7 post liquefaction part that lower tower uprising gas enters main distillation column 6 returns lower tower, another part through subcooler 4 cross cold after enter upper tower 8 top and participate in rectifying, the direct emptying of on-condensible gas.The oxygen cooling box 2 after subcooler 4, main heat exchanger 3 re-heat taken out bottom upper tower 8; The dirty nitrogen of the upper tower 8 top taking-up of main distillation column 6 is by dirty channel of nitrogen 11 cooling box 2 after subcooler 4, main heat exchanger 3 re-heat; The nitrogen that auxiliary tower 9 top is taken out is by channel of nitrogen 10 cooling box 2 after subcooler 4, main heat exchanger 3 re-heat.
Can find out, in this air separation unit, nitrogen is taken out by the auxiliary top of tower of main distillation column, auxiliary tower diameter causes circulation area significantly to reduce much smaller than Shang Ta, and the channel of nitrogen such as subcooler, main heat exchanger circulation area is also design than 1:1 by nitrogen oxygen, nitrogen output cannot be made to be greatly improved by general operational means such as varying duties.
In Fig. 2, a compressed air part through purification in this method enters ice chest 2 after booster expansion turbine group 1 supercharging, expand through booster expansion turbine group 1 after main heat exchanger 3 tentatively cooling again and lower the temperature, the middle and upper part directly sending into the upper tower 8 of main distillation column 6 through main heat exchanger 3, subcooler 4 after lowering the temperature participates in rectifying; The lower tower 5 that another part directly sends into main distillation column 6 after main heat exchanger 3 is lowered the temperature participates in rectifying.The liquid air that lower tower bottom takes out enters in the middle part of upper tower 8 and participates in rectifying after subcooler 4 is excessively cold; The condenser/evaporator 7 post liquefaction part that lower tower uprising gas enters main distillation column 6 returns lower tower, another part through subcooler 4 cross cold after enter upper tower 8 top and participate in rectifying, the direct emptying of on-condensible gas.The oxygen cooling box 2 after subcooler 4, main heat exchanger 3 re-heat taken out bottom upper tower 8; It is identical with the height and position of tower upper in former method that dirty nitrogen takes out height and position, but after subcooler 4, main heat exchanger 3 re-heat, enter former dirty nitrogen pipeline again by former channel of nitrogen 10 after cooling box 2; Nitrogen is taken out by upper tower 8 top after increasing, but after subcooler 4, main heat exchanger 3 re-heat, enters former nitrogen pipeline again by former dirty channel of nitrogen 11 after cooling box 2.
Citing is described: former design nitrogen oxygen product ratio is the 20000Nm of 1:1
3the upper tower height degree of/h air separation unit is 30440mm, and diameter is 2700mm, and auxiliary tower height degree is 4579mm, and diameter is 1920mm.After excising auxiliary tower, upper tower is increased 9150mm, make total height reach 39590mm, diameter is still 2700mm, and the height that upper tower increases is about 30.06% of former height.Upper tower increases rear dirty nitrogen, and to take out open height constant, nitrogen takes out that mouth is corresponding increases 9150mm, nitrogen, dirty nitrogen takes out through subcooler, tower is gone out after main heat exchanger re-heat, due to nitrogen in former air separation unit, dirty nitrogen pipeline diameter is respectively φ 508mm and φ 813mm, improve nitrogen oxygen ratio when oxygen withdrawal amount is constant and increase nitrogen withdrawal amount exactly, circulating resistance is not increased and just must increase pipe diameter, in view of nitrogen withdrawal amount increases the actual conditions of the rear corresponding minimizing of dirty nitrogen withdrawal amount, in air separation unit from tower nitrogen, dirty nitrogen is taken out mouthful place and is carried out gas channel switching, namely nitrogen utilizes former dirty nitrogen pipeline to carry out heat exchange and conveying, dirty nitrogen then utilizes former nitrogen pipeline to carry out heat exchange and conveying, nitrogen, former pipeline is switched to again after dirty nitrogen cooling box, after meeting the raising of nitrogen oxygen ratio, each medium circulating resistance is constant, do not affect nitrogen, dirty nitrogen heat exchange efficiency, save pipeline and subcooler, main heat exchanger carries out the expense transformed or change.
Claims (2)
1. improve a device for air separation unit nitrogen oxygen product ratio, comprise main heat exchanger, decompressor, subcooler, main distillation column, ice chest, it is characterized in that, described main distillation column is only provided with lower tower, condenser/evaporator, Shang Ta, and making while cancelling auxiliary tower, the basis of tower tower height degree on former increases by 30%; Upper tower is directly connected with nitrogen pipeline, nitrogen in ice chest, dirty stream of nitrogen gas passage are carrying out mutual switching with upper tower junction, namely nitrogen utilizes former dirty nitrogen pipeline to carry out heat exchange and conveying, dirty nitrogen then utilizes former nitrogen pipeline to carry out heat exchange and conveying, switches to former pipeline again after nitrogen, dirty nitrogen cooling box.
2. the device improving air separation unit nitrogen oxygen product ratio as claimed in claim 1, it is characterized in that, a compressed-air actuated part through purifying is through decompressor pressuring expansion, again after main heat exchanger, subcooler cooling, enter tower on main fractionating tower and participate in rectifying, another part directly enters tower under main fractionating tower through main heat exchanger and participates in rectifying; Lower tower bottom liquid air enters in the middle part of upper tower through subcooler and participates in rectifying, and lower top of tower nitrogen enters the condenser/evaporator post liquefaction of main distillation column, and a part is back to lower tower, and another part enters upper top of tower through subcooler and participates in rectifying, and fixed gas is directly emptying; Oxygen cooling box after subcooler, main heat exchanger re-heat that upper tower bottom is extracted out, after dirty nitrogen is still taken out by upper tower middle and upper part, utilize former nitrogen pipeline through subcooler, main heat exchanger re-heat access former dirty nitrogen pipeline after transferring out ice chest again, nitrogen is then taken out by the upper tower top after increasing, and utilizes former dirty nitrogen pipeline through subcooler, main heat exchanger re-heat access former nitrogen pipeline again after transferring out ice chest.
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| CN201310237929.1A CN103277981B (en) | 2013-06-14 | 2013-06-14 | Device and method for increasing nitrogen-to-oxygen ratio of air separation unit |
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| CN201310237929.1A CN103277981B (en) | 2013-06-14 | 2013-06-14 | Device and method for increasing nitrogen-to-oxygen ratio of air separation unit |
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| CN103277981A CN103277981A (en) | 2013-09-04 |
| CN103277981B true CN103277981B (en) | 2015-05-06 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3327394A2 (en) | 2016-11-25 | 2018-05-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for increasing low pressure pure nitrogen production by revamping original apparatus for cryogenic air separation |
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| CN103776239B (en) * | 2014-01-13 | 2016-03-30 | 浙江海天气体有限公司 | Multi-functional nitrogen-making device |
| CN104034123B (en) * | 2014-06-27 | 2016-05-18 | 莱芜钢铁集团有限公司 | A kind of air-separating plant hydrops is adjusted pure integration operation method |
| CN104949471A (en) * | 2015-05-14 | 2015-09-30 | 马钢(集团)控股有限公司 | Method for improving nitrogen yield of air separation device |
| CN109764639A (en) * | 2018-12-29 | 2019-05-17 | 上海华林工业气体有限公司 | A kind of HYCO ice chest reduces the System and method for of emptying |
| CN111268658B (en) * | 2020-03-11 | 2024-03-22 | 苏州市兴鲁空分设备科技发展有限公司 | Argon tail gas recovery and purification method and system |
| CN114459205A (en) * | 2022-02-22 | 2022-05-10 | 开封黄河空分集团有限公司 | Cooling system for expanded air |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2750269Y (en) * | 2004-10-28 | 2006-01-04 | 苏州市兴鲁空分设备科技发展有限公司 | Air separation device |
| US20080223077A1 (en) * | 2007-03-13 | 2008-09-18 | Neil Mark Prosser | Air separation method |
| CN201367351Y (en) * | 2009-03-17 | 2009-12-23 | 四川空分设备(集团)有限责任公司 | Device for preparing high purity oxygen |
| CN101886871B (en) * | 2010-08-04 | 2012-08-08 | 四川空分设备(集团)有限责任公司 | Method and device for producing pressure oxygen by air separation |
| CN202119205U (en) * | 2011-06-13 | 2012-01-18 | 开封空分集团有限公司 | Air separating device capable of alternately producing nitrogen and liquid nitrogen |
| US20130139547A1 (en) * | 2011-12-05 | 2013-06-06 | Henry Edward Howard | Air separation method and apparatus |
| CN202599013U (en) * | 2012-04-26 | 2012-12-12 | 上海启元空分技术发展股份有限公司 | Device for producing low purity oxygen with pressure and high purity nitrogen through backflow expansion refrigeration |
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2013
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3327394A2 (en) | 2016-11-25 | 2018-05-30 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for increasing low pressure pure nitrogen production by revamping original apparatus for cryogenic air separation |
| EP3327394A3 (en) * | 2016-11-25 | 2018-11-07 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for increasing low pressure pure nitrogen production by revamping original apparatus for cryogenic air separation |
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| CN103277981A (en) | 2013-09-04 |
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