CN103277981A - 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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- CN103277981A CN103277981A CN2013102379291A CN201310237929A CN103277981A CN 103277981 A CN103277981 A CN 103277981A CN 2013102379291 A CN2013102379291 A CN 2013102379291A CN 201310237929 A CN201310237929 A CN 201310237929A CN 103277981 A CN103277981 A CN 103277981A
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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 that improves air separation unit nitrogen oxygen product ratio.
Background technology
In recent years, along with the maximization of metallurgy industry blast furnace, converter and applying of oxygen-rich smelting technology, bigger variation has taken place to the demand percentage of oxygen, nitrogen in smelter, mainly show as growth to the nitrogen demand greater than the growth to oxygen demand, according to rough Statistics, nitrogen oxygen has original 1:1 than demand, has brought up to 1.2:1 or higher.But former supporting air separation unit nitrogen oxygen product ratio when design of producing oxygen, nitrogen is generally 1:1, and does not have big change substantially in the output of put into operation back oxygen, nitrogen product.If newly-built nitrogen oxygen product ratio substitutes existing equipment greater than the oxygen generating plant of 1:1, existing equipment leaves unused and has caused waste so; If according to the newly-built equipment of making nitrogen of nitrogen breach, certainly will to cause the significantly raising of production cost so.And still do not have effective reforming mode at present, to satisfy present oxygen nitrogen than the variation of demand.
As everyone knows, oxygen content in the atmosphere (on the volume) accounts for 20.9%, and nitrogen content (on the volume) accounts for 78.1%.When air separation unit nitrogen oxygen product ratio is 1:1, dirty nitrogen output then is 57.2%, also want many for 2 times of nitrogen output, just for existing air separation unit equipment component is transformed, the exchange of nitrogen, dirty stream of nitrogen gas passage provides condition with raising nitrogen oxygen product ratio for this.
Summary of the invention
Purpose of the present invention can't effectively satisfy oxygen nitrogen than changing for solving existing air separation unit exactly, and lack the problem of effective reforming mode, a kind of device and method that improves air separation unit nitrogen oxygen product ratio is provided, it is on existing air separation unit basis, and do not increase substantially under the situation of energy consumption, satisfy the 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 that improves air separation unit nitrogen oxygen product ratio, comprise main heat exchanger, decompressor, subcooler, main distillation column, ice chest, described main distillation column only is provided with down tower, condenser/evaporator, last tower, make the basis increase about 30% of tower tower height degree on former in the time of the auxilliary tower of cancellation, last tower directly is connected with nitrogen pipeline, the nitrogen in the ice chest, dirty stream of nitrogen gas passage is carrying out mutual switching with last tower junction, and 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, switch to former pipeline again behind the dirty nitrogen cooling box.
Compressed-air actuated part process decompressor pressuring expansion through purification after main heat exchanger, subcooler cooling, enters tower participation rectifying on the main fractionating tower again, and another part directly enters tower participation rectifying under the main fractionating tower through main heat exchanger; Following tower bottom liquid air enters the tower middle part through subcooler and participates in rectifying, and after following top of tower nitrogen entered the condenser/evaporator liquefaction of main distillation column, a part was back to down tower, and another part enters top of tower through subcooler and participates in rectifying, the direct emptying of fixed gas; Oxygen cooling box after subcooler, main heat exchanger re-heat that last tower bottom is extracted out, dirty nitrogen is still taken out by last tower middle and upper part, but gas channel and stream of nitrogen gas passage switch in the ice chest, behind subcooler, main heat exchanger cooling box, switch and insert former dirty nitrogen pipeline, nitrogen is then taken out by the top that the last tower that has increased under the constant situation of the equivalent number of plates substitutes original auxilliary tower, gas channel correspondingly switches with dirty stream of nitrogen gas passage in the ice chest, switches to insert former nitrogen pipeline behind subcooler, main heat exchanger cooling box.
A kind of method that adopts the raising nitrogen oxygen product ratio that improves air separation unit nitrogen oxygen product proportioning device makes tower basis increase of tower height degree on former about 30% in the time of the auxilliary tower of cancellation, it is original more than 2 times that tower nitrogen taking-up amount is brought up to; Increase the actual conditions that the dirty nitrogen amount in back descends according to nitrogen taking-up amount, with nitrogen, dirty nitrogen carries out the mutual switching of gas channel from taking-up place of last tower, be that 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, existing pipeline and heat transmission equipment had both been taken full advantage of, saved again because of nitrogen taking-up amount increase back pipeline modification, subcooler and main heat exchanger heat exchange area change changes the expense increase that causes, and behind cooling box, correspondingly switch to former pipeline, the nitrogen oxygen product ratio that makes whole air separation unit by 1:1 brought up to 2:1 and more than.
The invention has the beneficial effects as follows: do not increasing substantially under the condition of operating cost, the mutual switching of increasing transformation and nitrogen, dirty stream of nitrogen gas passage by tower on the air separation unit, realized air separation unit nitrogen oxygen product ratio by 1:1 bring up to 2:1 and more than, saved the idle waste that causes of the newly-built air separation unit occupation of capital and used equipment.20000Nm for example
3After/h grade air separation unit improved nitrogen oxygen product ratio, nitrogen output was by 20000Nm
3/ h brings up to 60000Nm
3/ h is by confessing 0.01 yuan/m of profit
3Calculate, can increase profit the whole year and be: (60000-20000) * ten thousand yuan of 365 * 24 * 0.01=350.4.
Description of drawings
Fig. 1 has air separation unit oxygen nitrogen production process chart now;
Fig. 2 air separation unit oxygen of the present invention nitrogen production process chart;
1. booster expansion turbine groups among the figure, 2. ice chest, 3. main heat exchanger, 4. subcooler 5. descends tower, 6. main distillation column, 7. condenser/evaporator is 8. gone up tower, 9. auxilliary tower, 10. channel of nitrogen, 11. dirty channel of nitrogen.
The specific embodiment
The present invention will be further described below in conjunction with accompanying drawing:
Among Fig. 1, compressed air part through purifying enters ice chest 2 after 1 supercharging of booster expansion turbine group, again through booster expansion turbine group 1 cooling of expanding, the last tower 8(through directly sending into main distillation column 6 after main heat exchanger 3, subcooler 4 coolings goes up tower 8 tower height degree basis on former and increases 30% after the preliminary cooling of main heat exchanger 3) middle and upper part participation rectifying; Another part is directly sent into main distillation column 6 after main heat exchanger 3 coolings following tower 5 participates in rectifying.The liquid air that following tower bottom takes out enters tower 8 middle parts and participates in rectifying after subcooler 4 mistakes are cold; Following tower uprising gas enters the condenser/evaporator 7 liquefaction back part of main distillation column 6 and returns tower down, and another part is crossed through subcooler 4 and entered the participation rectifying of tower 8 tops, the direct emptying of on-condensible gas after cold.Oxygen cooling box 2 after subcooler 4, main heat exchanger 3 re-heats that take out last tower 8 bottoms; The dirty nitrogen that take out at last tower 8 tops of main distillation column 6 is by dirty channel of nitrogen 11 cooling box 2 after subcooler 4, main heat exchanger 3 re-heats; The nitrogen that take out at auxilliary tower 9 tops is by channel of nitrogen 10 cooling box 2 after subcooler 4, main heat exchanger 3 re-heats.
As can be seen, in this air separation unit, nitrogen is taken out by the auxilliary top of tower of main distillation column, auxilliary tower diameter causes circulation area significantly to dwindle much smaller than Shang Ta, and channel of nitrogen such as subcooler, main heat exchanger circulation area also is to design than 1:1 by nitrogen oxygen, can't nitrogen output is greatly improved by general operational means such as varying duties.
Among Fig. 2, compressed air part through purifying in this method enters ice chest 2 after 1 supercharging of booster expansion turbine group, expand through booster expansion turbine group 1 after main heat exchanger 3 preliminary coolings again and lower the temperature, the middle and upper part of directly sending into the last tower 8 of main distillation column 6 after main heat exchanger 3, subcooler 4 coolings participates in rectifying; Another part is directly sent into main distillation column 6 after main heat exchanger 3 coolings following tower 5 participates in rectifying.The liquid air that following tower bottom takes out enters tower 8 middle parts and participates in rectifying after subcooler 4 mistakes are cold; Following tower uprising gas enters the condenser/evaporator 7 liquefaction back part of main distillation column 6 and returns tower down, and another part is crossed through subcooler 4 and entered the participation rectifying of tower 8 tops, the direct emptying of on-condensible gas after cold.Oxygen cooling box 2 after subcooler 4, main heat exchanger 3 re-heats that take out last tower 8 bottoms; The height and position of tower was identical on dirty nitrogen took out in height and position and the former method, but by former channel of nitrogen 10 through entering former dirty nitrogen pipeline again behind the cooling box 2 after subcooler 4, main heat exchanger 3 re-heats; Nitrogen is taken out by last tower 8 tops after increasing, but by former dirty channel of nitrogen 11 through entering former nitrogen pipeline again behind the cooling box 2 after subcooler 4, main heat exchanger 3 re-heats.
Describe for example: former design nitrogen oxygen product ratio is the 20000Nm of 1:1
3The last tower height degree of/h air separation unit is 30440mm, and diameter is 2700mm, and auxilliary tower height degree is 4579mm, and diameter is 1920mm.Behind the auxilliary tower of excision, will go up tower and increase 9150mm, and make total height reach 39590mm, diameter still is 2700mm, and the height that last tower increases is about 30.06% of former height.Last tower increases the dirty nitrogen in back, and to take out open height constant, nitrogen is taken out mouthful corresponding 9150mm of increasing, nitrogen, dirty nitrogen takes out through subcooler, go out tower after the main heat exchanger re-heat, because nitrogen in the former air separation unit, dirty nitrogen pipeline diameter is respectively φ 508mm and φ 813mm, under the constant situation of oxygen taking-up amount, improve nitrogen oxygen ratio and increase nitrogen taking-up amount exactly, circulating resistance is not just increased to increase pipe diameter, in view of increasing the dirty nitrogen taking-up in back, nitrogen taking-up amount measures the actual conditions of corresponding minimizing, in air separation unit from tower nitrogen, dirty nitrogen is taken out a mouthful place and is carried out the gas channel switching, be that 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, switch to former pipeline again behind the dirty nitrogen cooling box, it is constant to have satisfied each medium circulating resistance of nitrogen oxygen ratio raising back, do not influence nitrogen, dirty nitrogen heat exchange efficiency has been saved pipeline and subcooler, the expense that main heat exchanger is transformed or changed.
Claims (3)
1. a device that improves air separation unit nitrogen oxygen product ratio comprises main heat exchanger, decompressor, subcooler, main distillation column, ice chest, it is characterized in that described main distillation column only is provided with down tower, condenser/evaporator, Shang Ta, make tower increase by 30% in the basis of tower height degree on former in the time of the auxilliary tower of cancellation; Last tower directly is connected with nitrogen pipeline, nitrogen, dirty stream of nitrogen gas passage in the ice chest are carrying out mutual switching with last tower junction, be that 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 behind nitrogen, the dirty nitrogen cooling box.
2. the device of raising air separation unit nitrogen oxygen product ratio as claimed in claim 1, it is characterized in that, compressed-air actuated part through purifying is through the decompressor pressuring expansion, again after main heat exchanger, subcooler cooling, enter tower participation rectifying on the main fractionating tower, another part directly enters tower participation rectifying under the main fractionating tower through main heat exchanger; Following tower bottom liquid air enters the tower middle part through subcooler and participates in rectifying, and after following top of tower nitrogen entered the condenser/evaporator liquefaction of main distillation column, a part was back to down tower, and another part enters top of tower through subcooler and participates in rectifying, the direct emptying of fixed gas; Oxygen cooling box after subcooler, main heat exchanger re-heat that last tower bottom is extracted out, after dirty nitrogen is still taken out by last tower middle and upper part, utilize former nitrogen pipeline to insert former dirty nitrogen pipeline again through subcooler, main heat exchanger re-heat and after transferring out ice chest, nitrogen is then taken out by the top of the last tower after increasing, and utilizes former dirty nitrogen pipeline to insert former nitrogen pipeline again through subcooler, main heat exchanger re-heat and after transferring out ice chest.
3. method that adopts the raising nitrogen oxygen product ratio of claim 1 or 2 described raising air separation unit nitrogen oxygen product proportioning devices, it is characterized in that, make tower increase by 30% in the basis of tower height degree on former in the time of the auxilliary tower of cancellation, make tower nitrogen taking-up amount bring up to original 2 times or more than; Increase the actual conditions that the dirty nitrogen amount in back descends according to nitrogen taking-up amount, with nitrogen, dirty nitrogen carries out the mutual switching of gas channel from taking-up place of last tower, be that 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, existing pipeline and heat transmission equipment had both been taken full advantage of, saved again because of nitrogen taking-up amount increase back pipeline modification, subcooler and main heat exchanger heat exchange area change changes the expense increase that causes, and behind cooling box, correspondingly switch to former pipeline, the nitrogen oxygen product ratio that makes whole air separation unit by 1:1 brought up to 2:1 and more than.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103776239A (en) * | 2014-01-13 | 2014-05-07 | 浙江海天气体有限公司 | Multifunctional nitrogen making device |
| CN104034123A (en) * | 2014-06-27 | 2014-09-10 | 莱芜钢铁集团有限公司 | Liquid loading and purity regulating integration operation method of air separation plant |
| 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 |
| CN106949708A (en) * | 2016-11-25 | 2017-07-14 | 乔治洛德方法研究和开发液化空气有限公司 | A kind of method for being reequiped to improve Low Voltage Pure nitrogen output to original cryogenic air separation plant |
| 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 |
| CN111268658A (en) * | 2020-03-11 | 2020-06-12 | 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 |
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| CN106949708A (en) * | 2016-11-25 | 2017-07-14 | 乔治洛德方法研究和开发液化空气有限公司 | A kind of method for being reequiped to improve Low Voltage Pure nitrogen output to original cryogenic air separation plant |
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| 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 |
| CN111268658A (en) * | 2020-03-11 | 2020-06-12 | 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 |
| 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 |
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| CN103277981B (en) | 2015-05-06 |
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