CN204240704U - A kind of air separation unit with the air inlet of supplementary pressure nitrogen - Google Patents
A kind of air separation unit with the air inlet of supplementary pressure nitrogen Download PDFInfo
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- CN204240704U CN204240704U CN201420650913.3U CN201420650913U CN204240704U CN 204240704 U CN204240704 U CN 204240704U CN 201420650913 U CN201420650913 U CN 201420650913U CN 204240704 U CN204240704 U CN 204240704U
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Abstract
The utility model discloses a kind of air separation unit with the air inlet of supplementary pressure nitrogen, comprise one-level rectifying column, two-stage rectification tower, condenser/evaporator, heat exchanger, subcooler, provide the pressure nitrogen pipe network of supplementary pressure nitrogen to be connected through the top of heat exchanger with one-level rectifying column; Raw air close to liquefaction point is connected with one-level rectifying column; Go liquefied air to be connected with one-level rectifying column by the liquefied liquia air of cold acquisition of cold fluid at heat exchanger, the top of described one-level rectifying column is connected by condenser/evaporator with the bottom of two-stage rectification tower.Adopt this programme can obtain more nitrogen product; Also pressure oxygen can be obtained.The utility model overcomes the shortcoming of conventional nitrogen cycle, combines the advantage of air liquefaction heat exchange, avoids the shortcoming of producing nitrogen ability and reducing, is suitable for multiple device.
Description
Technical field
The utility model relates to a kind of air separation unit, that one effectively can increase nitrogen output, improve oxygen extraction ratio, especially significantly can reduce energy consumption and the air-separating plant of simple possible for when nitrogen oxygen yield higher, be specially the air separation unit of supplementary pressure nitrogen air inlet.
Background technology
Industrial expansion makes production technology progressively diversified, and the production capacity of user to air separation unit it is also proposed more requirement.The energy consumption of the whole technological process of nitrogen oxygen comparison that air separation unit exports and device will produce important impact.In conventional empty point flow process, by the restriction of oxygen extraction ratio, required air quantity can increase with the increase of oxygen making amount, thus energy consumption is increased, due to equipment longtime running, energy-conservation also just most important.
Some chemical process being in great demand to nitrogen, as synthetic ammonia, olefin hydrocarbon making by coal etc., oxygen nitrogen is extremely uneven, the rich nitrogen hunger of old process oxygen, and the separation power of oxygen is larger than nitrogen, and oxygen emptying energy consumption increases significantly.The pressure of some technological requirement nitrogen is very high, and specification is more, and nitrogen is according to external compression, and pressure match is difficult; Elevated pressure nitrogen compression easily suffocates because of nitrogen, leaks and easily causes security incident, and applying unit does not recommend elevated pressure nitrogen to adopt external compression; Nitrogen flow is little, and pressure height adopts piston compression to need standby host and changes consumable accessory to be safeguarded complicated, and turbo compressor efficiency is low and sometimes cannot realize; Chemical plant installations sky point compresses because generally adopting in oxygen for security consideration, and downsize in partial devices oxygen little, pressurized air flow is few, and in nitrogen, compressed nitrogen output can improve pressurized air flow; The chemical industry air separation unit of upper scale generally adopts steam drive one drag two, user does not wish too much compressor, some technological requirement nitrogen product pressure specification is more, according to external compression, and pressure match difficulty, if matching pressure, then the too much investment cost of compressor is high, and maintenance cost is high, the reliability of influential system, and need to consume a large amount of electric power, electricity drives costly.
General chemical industry air separation unit user recommends to adopt compression in nitrogen, and according to regular air liquefaction flow path, nitrogen output sharply declines, and gaseous air rectifying generally only can obtain the pressure nitrogen of 40 ~ 47%; According to nitrogen cycle nitrogen liquefaction flow path: cold damage is large, internal circulating load is large, and nitrogen pressure requirements is higher, and with nitrogen product pressure match difficulty, elevated pressure nitrogen compression has certain leakage and to suffocate security risk.The long equipment of nitrogen cycle pipeline is more, and nitrogen purity requirement is high, and need to replace for a long time, nitrogen purity is slowly qualified.
Another kind of situation is that liquid space division needs more nitrogen product, adopts regular air circulation not meet the demands, and user is reluctant to take the liquid space division device of conventional nitrogen cycle.
Summary of the invention
The utility model, just for above technical problem, provides one effectively can improve oxygen extraction ratio, reduces the air separation unit of energy consumption, supplementary pressure nitrogen air inlet easy and simple to handle.Employing this programme can obtain more nitrogen product simultaneously and liquid form product is stored as subsequent use, and thus obtained liquid oxygen is also by obtaining pressure oxygen with pressurized air heat exchange after liquid level difference or liquid oxygen pump supercharging; Obtain the liquid nitrogen supplemented also to pressurize and air heat-exchange by liquid nitrogen pump, obtain the interior compressed nitrogen of more high pressure.
Concrete technical scheme is as follows:
With an air separation unit for supplementary pressure nitrogen air inlet, comprise one-level rectifying column 1, two-stage rectification tower 2, condenser/evaporator 3, heat exchanger 4, subcooler 5, provide the pressure nitrogen pipe network of supplementary pressure nitrogen to be connected through the top of heat exchanger 4 with one-level rectifying column; The pipeline of air 8 of supplying raw materials is connected with one-level rectifying column 1; The pipeline of liquefied air 9 is provided to connect heat exchanger 4, the described liquefied air 9 that goes was liquefied cold acquisition liquid air 10 in heat exchanger 4, described heat exchanger 4 is connected with one-level rectifying column 1, and the top of described one-level rectifying column 1 is connected by condenser/evaporator 3 with the bottom of two-stage rectification tower 2.
Alternately, above-mentioned a kind of air separation unit with the air inlet of supplementary pressure nitrogen, the source of described supplementary pressure nitrogen is not limit, and both can derive from nitrogen compressor, also can derive from nitrogen pipe network.
Alternately, above-mentioned a kind of air separation unit with the air inlet of supplementary pressure nitrogen, is connected liquid oxygen pump 11 between condenser/evaporator 3 with heat exchanger 4.
Alternately, above-mentioned a kind of air separation unit with the air inlet of supplementary pressure nitrogen, the liquid nitrogen 12 of condenser/evaporator 3 condensation is connected with liquid nitrogen pump 20, and described liquid nitrogen pump 20 is connected with heat exchanger 4.
Alternately, above-mentioned a kind of air separation unit with the air inlet of supplementary pressure nitrogen, the liquid oxygen that described condenser/evaporator 3 obtains is connected with oxygen booster 22 by liquid oxygen hydrostatic column or liquid oxygen pump 11, and liquid oxygen evaporated form is for entirely to soak mode, and the oxygen outlet of described oxygen booster 22 is connected with heat exchanger 4.
In sum, owing to have employed technique scheme, the beneficial effects of the utility model are:
1, enter air separation unit by supplementary pressure nitrogen, and through main condenser evaporator condensation, increase the liquid nitrogen reflux amount of two-stage rectification tower, oxygen nitrogen and argon is separated more thorough, to obtain more nitrogen product, improves the yield of oxygen argon simultaneously.
2, the condensation of the utility model supplementary pressure nitrogen can obtain more liquid nitrogen, is convenient to realize compression in liquid nitrogen pump pressurized nitrogen.
3, the utility model is due to by outside nitrogen compressor supplementary pressure nitrogen, and tonifying Qi adjustable range is large, and oxygen nitrogen product proportion can flexible modulation, is convenient to realize rectifying Optimum Matching, makes energy consumption reach minimum; Old process is difficult to realize rectifying coupling, and oxygen nitrogen ratio is comparatively fixing, adjusts limited.
4, the utility model overcomes the shortcoming of compression in the circulation of conventional medium pressure nitrogen: nitrogen compression ratio air compressing energy consumption is high, and nitrogen is lower than air fluid heat-transmission, and nitrogen needs higher pressure than air and liquid oxygen heat exchange; It is large that elevated pressure nitrogen press leaks asphyxiation hazard, and the cold damage of nitrogen cycle is large; The utility model combines the advantage of air liquefaction heat exchange: supplementary nitrogen amount is less, and pressure is low, and heat exchanger process tolerance is few, and the cold damage of device is few, supercharging air good effect of heat exchange, and pressure is without the need to very high, and flow is little, and liquid air is easily absorbed process by two-stage rectification tower.
5, the utility model security is high: in oxygen nitrogen, compression still adopts supercharging air heat exchange, avoids the danger that elevated pressure nitrogen press leaks, and nitrogen compressor pressure is general lower, and risk of leakage is little.
6, in the utility model nitrogen, compression adopts supercharging air heat exchange, avoids the compression of small flow high pressure power poor efficiency, can increase air booster flow further, improve its compression efficiency, be also convenient to one drag two machine coupling.
7, the utility model is convenient to compression in nitrogen pump, is easy to overcome nitrogen product pressure and does not mate with compressor; Or nitrogen product pressure high flow capacity is little; User is reluctant that receiving piston nitrogen compressor or nitrogen compressor quantity are too much, and investment cost is high or floor space large, and maintenance workload is unsuitable for greatly the shortcoming of nitrogen external compression; Power consumption can be greatly reduced simultaneously.
8, the utility model is by simple process, avoids most of air separation unit to adopt medium pressure nitrogen circulation.
9, the utility model has process organization's optimization, and simply, equipment investment cost is low, and the displacement of nitrogen pipeline easily, starts fast, capable of reducing energy consumption.
Accompanying drawing explanation
The utility model illustrates by example and with reference to the mode of accompanying drawing, wherein:
Fig. 1 is supplementary pressure nitrogen air inlet in embodiment 1, the schematic diagram of compression air separation device in oxygen;
Fig. 2 is supplementary pressure nitrogen air inlet in embodiment 2, the schematic diagram of compression air separation device in oxygen nitrogen;
Fig. 3 is supplementary pressure nitrogen air inlet in embodiment 3, the schematic diagram of air circulating fluid air separation unit;
Fig. 4 is supplementary pressure nitrogen air inlet in embodiment 4, the schematic diagram of oxygen supercharging air separating device.
Reference numeral: 1 is one-level rectifying column, 2 is two-stage rectification tower, 3 is condenser/evaporator, 4 is heat exchanger, 5 is subcooler, 6 is supplementary pressure nitrogen, 7 is low temperature supplementary pressure nitrogen, 8 is raw air, 9 for removing liquefied air, 10 is liquid air, 11 is liquid oxygen pump, 12 is liquid nitrogen, 13 is oxygen-enriched liquid air, 14 is oxygen deprivation liquid air, 15 is nitrogen products, 16 is product liquid oxygen, 17 is low-pressure nitrogen, 18 is dirty nitrogen, 19 is interior compressed nitrogen, 20 is liquid nitrogen pump, 21 is interior compressed oxygen, 22 is oxygen booster.
Detailed description of the invention
All features disclosed in this description, or the step in disclosed all methods or process, except mutually exclusive feature and/or step, all can combine by any way.Below in conjunction with Figure of description and specific embodiment, the utility model is described in further detail.But this should be interpreted as that above-mentioned subject area of the present utility model is only limitted to following embodiment.
Embodiment 1:
A) raw air 8 is cooled to through heat exchanger 4 bottom sending into one-level rectifying column 1 close to liquefaction point.
B) go the air 9 liquefied to cool through heat exchanger 4, be mainly liquefied as by interior compression liquid oxygen the middle and lower part that liquid air 10 sends into one-level rectifying column 1.
C) in one-level rectifying column 1, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, more up in column plate, the heavy constituent of liquid air is fewer.Described one-level rectifying column 1 top obtains pure pressure nitrogen gas.
D) the supplementary pressure nitrogen 6 from pipe network cools through heat exchanger 4, obtain low temperature supplementary pressure nitrogen 7, enter one-level rectifying column 1 top, two strands of pressure nitrogen gas converge the condensation side entrance sending into condenser/evaporator 3, nitrogen, by liquid oxygen condensation, obtains liquid nitrogen 12 from condensation side outlet.
E) liquid nitrogen 12 that condenser/evaporator 3 outlet obtains is partly refluxed to one-level rectifying column 1 and participates in rectifying, and a part is sent into two-stage rectification tower 2 top and participated in rectifying after subcooler 5 cools.A part derives as nitrogen products 15.
F) one-level rectifying column 1 middle and lower part oxygen deprivation liquid air 14 is sent into two-stage rectification tower 2 top and is participated in rectifying after subcooler 5 cools.Oxygen-enriched liquid air 13 bottom one-level rectifying column 1 is sent into two-stage rectification tower 2 middle and upper part and is participated in rectifying after subcooler 5 cools.
G) in two-stage rectification tower 2, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, heavy constituent is washed down, and more up heavy constituent is fewer.Obtain low-pressure nitrogen at two-stage rectification tower 2, the liquid oxygen obtained bottom two-stage rectification tower 2 enters condenser/evaporator 3 is obtained two-stage rectification tower 2 upflowing vapor by the vaporized nitrogen at one-level rectifying column 1 top, simultaneously final acquisition product liquid oxygen 16.
H) liquid oxygen that condenser/evaporator 3 extracts is pressurizeed through liquid oxygen pump 11 or is entered compressed oxygen 21 in heat exchanger 4 re-heat acquisition by liquid oxygen difference in height (hydrostatic column) supercharging.
I) sending ice chest by becoming Room-temperature low-pressure nitrogen 17 after subcooler 5 and heat exchanger 4 re-heat successively from the low-pressure nitrogen of two-stage rectification tower 2 Base top contact, removing user's low pressure nitrogen pipe network.
The dirty nitrogen of the adjustment top nitrogen purity of j) drawing on two-stage rectification tower 2 top, successively by becoming the dirty nitrogen 18 of normal temperature after subcooler 5 and heat exchanger 4 re-heat, sends ice chest.
Embodiment 2:
A) raw air 8 is cooled to through heat exchanger 4 bottom sending into one-level rectifying column 1 close to liquefaction point.
B) go the air 9 liquefied to cool through heat exchanger 4, be mainly liquefied as by interior compression liquid oxygen the middle and lower part that liquid air 10 sends into one-level rectifying column 1.
C) in one-level rectifying column 1, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, more up in column plate, the heavy constituent of liquid air is fewer.Described one-level rectifying column 1 top obtains pure pressure nitrogen gas.
D) the supplementary pressure nitrogen 6 from pipe network cools through heat exchanger 4, obtain low temperature supplementary pressure nitrogen 7, enter one-level rectifying column 1 top, two strands of pressure nitrogen gas converge the condensation side entrance sending into condenser/evaporator 3, nitrogen, by liquid oxygen condensation, obtains liquid nitrogen 12 from condensation side outlet.
E) liquid nitrogen 12 that condenser/evaporator 3 outlet obtains is partly refluxed to one-level rectifying column 1 and participates in rectifying, and a part is sent into two-stage rectification tower 2 top and participated in rectifying after subcooler 5 cools.A part derives as nitrogen products 15.
F) one-level rectifying column 1 middle and lower part oxygen deprivation liquid air 14 is sent into two-stage rectification tower 2 top and is participated in rectifying after subcooler 5 cools.Oxygen-enriched liquid air 13 bottom one-level rectifying column 1 is sent into two-stage rectification tower 2 middle and upper part and is participated in rectifying after subcooler 5 cools.
G) in two-stage rectification tower 2, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, heavy constituent is washed down, and more up heavy constituent is fewer.Obtain low-pressure nitrogen at two-stage rectification tower 2, the liquid oxygen obtained bottom two-stage rectification tower 2 enters condenser/evaporator 3 is obtained two-stage rectification tower 2 upflowing vapor by the vaporized nitrogen at one-level rectifying column 1 top, simultaneously final acquisition product liquid oxygen 16.
H) liquid oxygen that condenser/evaporator 3 extracts is pressurizeed through liquid oxygen pump 11 or is entered compressed oxygen 21 in heat exchanger 4 re-heat acquisition by liquid oxygen difference in height (hydrostatic column) supercharging.
I) from the low-pressure nitrogen of two-stage rectification tower 2 Base top contact successively by after subcooler 5 and heat exchanger 4 re-heat, become Room-temperature low-pressure nitrogen and send ice chest, enter the dirty nitrogen 18 of the adjustment top nitrogen purity of drawing on two-stage rectification tower 2 top, sending ice chest by becoming Room-temperature low-pressure nitrogen 17 after subcooler 5 and heat exchanger 4 re-heat successively, removing user's low pressure nitrogen pipe network.
J) part liquid nitrogen that condenser/evaporator 3 condensation side obtains is pressurizeed through liquid nitrogen pump, and pressure nitrogen gas also enters compressed nitrogen 19 in heat exchanger 4 re-heat acquisition by liquefaction warp from supercharging (liquid nitrogen difference in height) supercharging.
Embodiment 3:
A) raw air 8 is cooled to through heat exchanger 4 bottom sending into one-level rectifying column 1 close to liquefaction point.
B) go the air 9 liquefied to cool through heat exchanger 4, be mainly liquefied as by interior compression liquid oxygen the middle and lower part that liquid air 10 sends into one-level rectifying column 1.
C) in one-level rectifying column 1, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, more up in column plate, the heavy constituent of liquid air is fewer.Described one-level rectifying column 1 top obtains pure pressure nitrogen gas.
D) the supplementary pressure nitrogen 6 from pipe network cools through heat exchanger 4, obtain low temperature supplementary pressure nitrogen 7, enter one-level rectifying column 1 top, two strands of pressure nitrogen gas converge the condensation side entrance sending into condenser/evaporator 3, nitrogen, by liquid oxygen condensation, obtains liquid nitrogen 12 from condensation side outlet.
E) liquid nitrogen 12 that condenser/evaporator 3 outlet obtains is partly refluxed to one-level rectifying column 1 and participates in rectifying, and a part is sent into two-stage rectification tower 2 top and participated in rectifying after subcooler 5 cools.A part derives as nitrogen products 15.
F) one-level rectifying column 1 middle and lower part oxygen deprivation liquid air 14 is sent into two-stage rectification tower 2 top and is participated in rectifying after subcooler 5 cools.Oxygen-enriched liquid air 13 bottom one-level rectifying column 1 is sent into two-stage rectification tower 2 middle and upper part and is participated in rectifying after subcooler 5 cools.
G) in two-stage rectification tower 2, gas from below to up carries out heat and mass with top-down liquid on column plate or filler; Through rectifying washing, heavy constituent is washed down, and more up heavy constituent is fewer.Obtain low-pressure nitrogen at two-stage rectification tower 2, the liquid oxygen obtained bottom two-stage rectification tower 2 enters condenser/evaporator 3 is obtained two-stage rectification tower 2 upflowing vapor by the vaporized nitrogen at one-level rectifying column 1 top, simultaneously final acquisition product liquid oxygen 16.
H) liquid oxygen product that condenser/evaporator 3 extracts goes user.
K) send ice chest by after subcooler 5 and heat exchanger 4 re-heat successively from the low-pressure nitrogen of two-stage rectification tower 2 Base top contact, become Room-temperature low-pressure nitrogen 17 and send ice chest, remove user's low pressure nitrogen pipe network.
The dirty nitrogen of the adjustment top nitrogen purity of i) drawing on two-stage rectification tower 2 top, successively by being the dirty nitrogen 18 of normal temperature after subcooler 5 and heat exchanger 4 re-heat, sends ice chest.
Embodiment 4:
Substantially similar embodiment 1, it is lower to be mainly used in oxygen pressure, is security consideration, and the evaporation of pressure oxygen adopts external oxygen booster 22 formula of bathing entirely to soak operation, instead of evaporates in heat exchanger 4.
The utility model is by taking the air separation unit of supplementary pressure nitrogen air inlet, the reflux ratio improving two-stage rectification tower improves the separation of oxygen nitrogen and argon, more nitrogen product and argon product can be obtained, make to consume less raw air under the condition of production equivalent oxygen, be particularly useful for the higher air separation unit of nitrogen oxygen yield simultaneously.There is process optimization, enforcement is simple, energy consumption is low, the advantage such as flexible adjustment, maximization of economic benefit.
The utility model is not limited to aforesaid detailed description of the invention.The utility model expands to any new feature of disclosing in this manual or any combination newly, and the step of the arbitrary new method disclosed or process or any combination newly.Step in all methods disclosed in this description or process, except mutually exclusive feature and/or step, all can combine by any way.Arbitrary feature disclosed in this description (comprising any accessory claim, summary and accompanying drawing), unless specifically stated otherwise, all can be replaced by other equivalences or the alternative features with similar object.Namely unless specifically stated otherwise, each feature is an example in a series of equivalence or similar characteristics.
Claims (4)
1. the air separation unit with the air inlet of supplementary pressure nitrogen, comprise one-level rectifying column (1), two-stage rectification tower (2), condenser/evaporator (3), heat exchanger (4), subcooler (5), it is characterized in that: provide the pressure nitrogen pipe network of supplementary pressure nitrogen to be connected with the top of one-level rectifying column through heat exchanger (4); The pipeline of air (8) of supplying raw materials is connected with one-level rectifying column (1); The pipeline of liquefied air (9) is provided to connect heat exchanger (4), the described liquefied air (9) that goes was liquefied cold acquisition liquid air (10) in heat exchanger (4), described heat exchanger (4) is connected with one-level rectifying column (1), and the top of described one-level rectifying column (1) is connected by condenser/evaporator (3) with the bottom of two-stage rectification tower (2).
2. a kind of air separation unit with the air inlet of supplementary pressure nitrogen as claimed in claim 1, is characterized in that: between condenser/evaporator (3) with heat exchanger (4), be connected liquid oxygen pump (11).
3. a kind of air separation unit with the air inlet of supplementary pressure nitrogen as claimed in claim 1 or 2, is characterized in that: the liquid nitrogen (12) of condenser/evaporator (3) condensation is connected with liquid nitrogen pump (20), and described liquid nitrogen pump (20) is connected with heat exchanger (4).
4. a kind of air separation unit with the air inlet of supplementary pressure nitrogen as claimed in claim 1 or 2, it is characterized in that: the liquid oxygen that described condenser/evaporator (3) obtains is connected with oxygen booster (22) by liquid oxygen difference in height or liquid oxygen pump (11), the oxygen outlet of described oxygen booster (22) is connected with heat exchanger (4); Described liquid oxygen evaporated form is for entirely to soak mode.
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| CN201420650913.3U CN204240704U (en) | 2014-11-04 | 2014-11-04 | A kind of air separation unit with the air inlet of supplementary pressure nitrogen |
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| CN201420650913.3U CN204240704U (en) | 2014-11-04 | 2014-11-04 | A kind of air separation unit with the air inlet of supplementary pressure nitrogen |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019127180A1 (en) * | 2017-12-28 | 2019-07-04 | 乔治洛德方法研究和开发液化空气有限公司 | Cryogenic rectification process-based method for producing air product, and air separation system |
| CN111928576A (en) * | 2020-08-14 | 2020-11-13 | 淄博盈德气体有限公司 | Air separation tower capable of controlling air inflow |
-
2014
- 2014-11-04 CN CN201420650913.3U patent/CN204240704U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019127180A1 (en) * | 2017-12-28 | 2019-07-04 | 乔治洛德方法研究和开发液化空气有限公司 | Cryogenic rectification process-based method for producing air product, and air separation system |
| CN111542723A (en) * | 2017-12-28 | 2020-08-14 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing air product based on cryogenic rectification process and air separation system |
| CN111542723B (en) * | 2017-12-28 | 2022-04-08 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing air product based on cryogenic rectification process and air separation system |
| CN111928576A (en) * | 2020-08-14 | 2020-11-13 | 淄博盈德气体有限公司 | Air separation tower capable of controlling air inflow |
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