CN205860657U - A kind of device of high-speed oxygen - Google Patents
A kind of device of high-speed oxygen Download PDFInfo
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- CN205860657U CN205860657U CN201620141093.4U CN201620141093U CN205860657U CN 205860657 U CN205860657 U CN 205860657U CN 201620141093 U CN201620141093 U CN 201620141093U CN 205860657 U CN205860657 U CN 205860657U
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Abstract
This utility model belongs to space division technique field, relates to the device of a kind of high-speed oxygen, and including the upper tower being sequentially connected with, condenser/evaporator, Xia Ta, oxygen evaporator, liquid oxygen storage tank, described condenser/evaporator is connected with oxygen evaporator top by pipeline f；It is connected with lower tower bottom by pipeline e bottom described oxygen evaporator；It is connected with liquid oxygen storage tank by pipeline a bottom described oxygen evaporator；Described liquid oxygen storage tank blows out pipeline h by pipeline c with the liquid bottom condenser/evaporator and is connected；On described pipeline c, connection has pipeline b；Described upper top of tower is provided with tower outlet；Described condenser/evaporator is provided with liquid nitrogen outlet；Use the oxygenerator of this structure, the air separation unit time in the hydrops stage gone into operation when producing can be shortened, thus reach quickly to produce the purpose of qualified oxygen and liquid oxygen, and realize energy-saving and cost-reducing and reduce production cost.
Description
Technical field
This utility model belongs to space division technique field, relates to the device of a kind of high-speed oxygen, is specially a kind of air separation unit curtailment of operation, can go out the flow scheme improvements of high-purity oxygen and liquid oxygen with Fast Purification.
Background technology
Air separation unit is to utilize air liquefaction the technique utilizing principles of rectification to obtain other gases such as high-purity oxygen.
Full low pressure air separation unit uses high-power compressor group by after air pressurized, again through expander refrigeration and a series of heat exchange process, being cooled to by the air of ambient temperature liquefies (minimum up to-193 DEG C) and enter rectifying column obtains final products after rectification.From the point of view of medium-and-large-sized air separation unit, normal oxygen preparation needs experience cooling, hydrops and the pure three phases of tune, and only three process minimum times are 36h.Cooling is to utilize the gas progressively lowered the temperature that the equipment and tower body that are in room temperature are progressively cooled to suitable operating mode, then create conditions for carrying out hydrops after gas liquefaction, hydrops is then to need to include other material such as oxygen-enriched liquid air, high-purity liquid oxygen at tower inner product liquid storage body, to realize the purpose that rectification separates and purifies high purity product, adjust pure, be that the rectifying column having reached rectification operating mode carries out the tune of product is pure.The three above stage is that air separation unit reaches normally to produce be subjected to process, but, the power consumption per hour of air separation unit is the most surprising, it is possible to the effective curtailment of operation is particularly important for reducing production cost and energy efficient.Cooling and adjust pure stage human intervention degree relatively low, the hydrops stage then can carry out flow scheme improvements and reach energy-saving and cost-reducing purpose with the shortening time.
Summary of the invention
The present invention seeks to the device by designing a kind of high-speed oxygen, including the upper tower being sequentially connected with, condenser/evaporator, Xia Ta, oxygen evaporator, liquid oxygen storage tank；The bottom of described upper tower is joined directly together with condenser/evaporator；Described condenser/evaporator is connected with lower top of tower by pipeline d；Described condenser/evaporator is connected with oxygen evaporator top by pipeline f；It is connected with lower tower bottom by pipeline e bottom described oxygen evaporator；It is connected with liquid oxygen storage tank by pipeline a bottom described oxygen evaporator；Described liquid oxygen storage tank blows out pipeline h by pipeline c with the liquid bottom condenser/evaporator and is connected；Use the oxygenerator of this structure, the air separation unit time in the hydrops stage gone into operation when producing can be shortened, thus reach quickly to produce the purpose of qualified oxygen and liquid oxygen, and realize energy-saving and cost-reducing and reduce production cost.
To achieve these goals, the technical scheme that the present invention takes is as follows:
The device of a kind of high-speed oxygen, including the upper tower being sequentially connected with, condenser/evaporator, Xia Ta, oxygen evaporator, liquid oxygen storage tank；The bottom of described upper tower is joined directly together with condenser/evaporator；Described condenser/evaporator is connected with lower top of tower by pipeline d；Described condenser/evaporator is connected with oxygen evaporator top by pipeline f；It is connected with lower tower bottom by pipeline e bottom described oxygen evaporator；It is connected with liquid oxygen storage tank by pipeline a bottom described oxygen evaporator；Described liquid oxygen storage tank blows down pipeline h by pipeline c with the liquid bottom condenser/evaporator and is connected；On described pipeline c, connection has pipeline b；Described upper top of tower is provided with tower outlet；Described condenser/evaporator is provided with liquid nitrogen outlet；Pipeline h it is provided with bottom described condenser/evaporator；Described condenser/evaporator is internally provided with 1# plate-fin heat exchanger；Described oxygen evaporator top is provided with oxygen evaporator outlet；Described oxygen evaporator is provided with air intlet；Described oxygen evaporator is internally provided with 2# plate-fin heat exchanger；It is provided with low temperature reciprocating pump on described pipeline c；Described upper top of tower is provided with expanded air import；Described pipeline a, b, c, g, h are provided with control valve.
During use, pipeline a, b, the control valve of c is first closed, pipeline g, control valve on h is all opened, raw air is after cooling PROCESS FOR TREATMENT, the air of cooling enters its internal 1# plate-fin heat exchanger from the air intlet of oxygen evaporator and carries out heat exchange process, after heat exchange processes, gas enters into lower tower bottom by pipeline e, now process due to the heat-exchanging process in oxygen evaporator, its temperature has reached-173 DEG C, reach the condensing temperature of air, have portion gas to condense out and become oxygen-enriched liquid air, this oxygen-enriched liquid air is discharged being exported by the liquid air of lower tower bottom；Uncooled gas enters into condenser/evaporator by pipeline d after then rising the lower column overhead of arrival along lower column plate block-by-block, and passes through to pass through after its internal 2# plate-fin heat exchanger heat exchange processes liquid nitrogen outlet discharge.Swell refrigeration air will enter upper tower by expanded air import, can be that whole oxygenerator provides cold owing to its temperature is relatively low, after expanded air enters upper tower, liquid portion is dirty, after also passing through heat exchange (offer cold) in entering into oxygen evaporator by pipeline f after heat exchange in condenser/evaporator (offer cold), gas is discharged from oxygen evaporator outlet, and liquid oxygen is entered liquid oxygen storage tank by pipeline a；Gas part then rises through successively filler, is discharged by the outlet of upper tower.Cooling through said process processes, and during until the temperature in condenser/evaporator reaches-180 DEG C (oxygen liquid is melted into the preference temperature for high-purity liquid oxygen), chilling temperature condition just reaches qualified.
Pipeline a is the passage that the liquid oxygen before stopping enters liquid oxygen storage tank.Enough liquid oxygen have been had for driving or from liquefied oxygen tank vehicle, liquid oxygen can be squeezed into liquid oxygen storage tank by pipeline b in production before, liquid oxygen storage tank.When liquid oxygen storage tank has enough liquid oxygen, need to open the valve on pipeline c, the valve closing on liquid blowout pipeline h, and start low temperature reciprocating pump 6, the liquid oxygen in liquid oxygen storage tank is driven in condenser/evaporator by pipeline c and h.This process can accelerate the accumulation of liquid oxygen, and provides enough colds to make condenser/evaporator and oxygen evaporator carry out heat exchange, and makes operating mode reach process conditions.Just can close low temperature reciprocating pump the valve blinding off a line on c when the liquid oxygen face height in condenser/evaporator reaches 3300mm, and the liquid oxygen in condenser/evaporator is adjusted pure process, simultaneously because the squeezing into so that adjusting the pure stage easily to operate of high-purity liquid oxygen.When liquid oxygen liquid oxygen face, height reaches 3300mm, and heat exchanger can be made entirely to soak to ensure the heat exchange area having abundance, and clashes into heat exchanger after being possible to prevent the solidification of the minimum gas such as acetylene and set off an explosion.The pure process of tune of the present utility model is prior art.
Prior art hydrops provides cold to be entered by expanded air import for the air after expanding, and condenses nitrogen, and heat exchange in oxygen evaporator in condenser/evaporator, owing to driving initial stage tower body and the higher hydrops of device temperature can be the slowest.Use the oxygenerator of this structure, through adding pipeline c after liquid oxygen storage tank and being connected in liquid discharge pipe h counter for the liquid oxygen operating procedure filling back condenser/evaporator fully achieves the time shortening air separation unit hydrops, thus reach quickly to produce the purpose of qualified oxygen and liquid oxygen, and realize energy-saving and cost-reducing and reduce production cost.
In sum, through adding pipeline c after liquid oxygen storage tank and being connected in liquid discharge pipe h counter for the liquid oxygen operating procedure filling back condenser/evaporator fully achieves the time shortening air separation unit hydrops, energy-saving and cost-reducing purpose has been reached.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram of a kind of high-speed oxygen；
In figure, 1 is upper tower, and 2 is condenser/evaporator, and 3 is lower tower, 4 is oxygen evaporator, and 5 is liquid oxygen storage tank, and 6 is low temperature reciprocating pump, and 7 is 1# plate-fin heat exchanger, 8 is 2# plate-fin heat exchanger, and 9 is air intlet, and 10 export for liquid air, and 11 is the outlet of upper tower, 12 export for oxygen evaporator, and 13 is expanded air import, and 14 is liquid nitrogen outlet, a, b, c, d, e, f, h are pipeline.
Detailed description of the invention
The device of a kind of high-speed oxygen, including the upper tower 1 being sequentially connected with, condenser/evaporator 2, lower tower 3, oxygen evaporator 4, liquid oxygen storage tank 5；The bottom of described upper tower 1 is joined directly together with condenser/evaporator 2；Described condenser/evaporator 2 is connected with lower tower 3 top by pipeline d；Described condenser/evaporator 2 is connected with oxygen evaporator 4 top by pipeline f；It is connected bottom lower tower 3 by pipeline e bottom described oxygen evaporator 4；It is connected with liquid oxygen storage tank 5 by pipeline a bottom described oxygen evaporator 4；Described liquid oxygen storage tank 5 blows out pipeline h by pipeline c with the liquid bottom condenser/evaporator 2 and is connected；On described pipeline c, connection has pipeline b；Described upper tower 1 top is provided with tower outlet 11；Described condenser/evaporator 2 is provided with liquid nitrogen outlet 14；Described condenser/evaporator 2 is internally provided with 1# plate-fin heat exchanger 7；Liquid air outlet 10 it is provided with bottom described lower tower 2；Described oxygen evaporator 4 top is provided with oxygen evaporator outlet 12；Described oxygen evaporator 4 is provided with air intlet 9；Described oxygen evaporator 4 is internally provided with 2# plate-fin heat exchanger 8；It is provided with low temperature reciprocating pump 6 on described pipeline c；Described upper tower 1 top is provided with expanded air import 13；Described pipeline a, b, c, f, h are provided with control valve.
Claims (4)
1. the device of a high-speed oxygen, including the upper tower (1) being sequentially connected with, condenser/evaporator (2), lower tower (3), oxygen evaporator (4), liquid oxygen storage tank (5), it is characterised in that: the bottom of described upper tower (1) is joined directly together with condenser/evaporator (2)；Described condenser/evaporator (2) is connected by pipeline d with Xia Ta (3) top；Described condenser/evaporator (2) is connected with oxygen evaporator (4) top by pipeline f；Described oxygen evaporator (4) bottom is connected by pipeline e with Xia Ta (3) bottom；Described oxygen evaporator (4) bottom is connected with liquid oxygen storage tank (5) by pipeline a；Described liquid oxygen storage tank (5) is connected with the liquid blowout pipeline h of condenser/evaporator (2) bottom by pipeline c；On described pipeline c, connection has pipeline b；Described upper tower (1) top is provided with nitrogen outlet (11)；Described condenser/evaporator (2) is provided with liquid nitrogen outlet (14)；Described lower tower (3) bottom is provided with liquid air outlet (10)；Described oxygen evaporator (4) top is provided with oxygen evaporator outlet (12)；Described oxygen evaporator (4) is provided with air intlet (9)；Low temperature reciprocating pump (6) it is provided with on described pipeline c；Described upper tower (1) top is provided with expanded air import (13).
2. the device of high-speed oxygen as claimed in claim 1, it is characterised in that: described condenser/evaporator (2) is internally provided with 1# plate-fin heat exchanger (7).
3. the device of high-speed oxygen as claimed in claim 1, it is characterised in that: described oxygen evaporator (4) is internally provided with 2# plate-fin heat exchanger (8).
4. the device of high-speed oxygen as claimed in claim 1, it is characterised in that；Described pipeline a, b, c, f, h are provided with control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620141093.4U CN205860657U (en) | 2016-02-25 | 2016-02-25 | A kind of device of high-speed oxygen |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620141093.4U CN205860657U (en) | 2016-02-25 | 2016-02-25 | A kind of device of high-speed oxygen |
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| CN205860657U true CN205860657U (en) | 2017-01-04 |
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| CN201620141093.4U Active CN205860657U (en) | 2016-02-25 | 2016-02-25 | A kind of device of high-speed oxygen |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109855388A (en) * | 2019-02-26 | 2019-06-07 | 中国神华能源股份有限公司 | Cryogenic technology device and cryogenic technology method |
| CN109974394A (en) * | 2019-04-23 | 2019-07-05 | 山东京博众诚清洁能源有限公司 | A kind of method that air-seperation system and its stage that goes into operation carry out hydrops |
-
2016
- 2016-02-25 CN CN201620141093.4U patent/CN205860657U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109855388A (en) * | 2019-02-26 | 2019-06-07 | 中国神华能源股份有限公司 | Cryogenic technology device and cryogenic technology method |
| CN109974394A (en) * | 2019-04-23 | 2019-07-05 | 山东京博众诚清洁能源有限公司 | A kind of method that air-seperation system and its stage that goes into operation carry out hydrops |
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