CN207729907U - The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification - Google Patents
The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification Download PDFInfo
- Publication number
- CN207729907U CN207729907U CN201721880887.3U CN201721880887U CN207729907U CN 207729907 U CN207729907 U CN 207729907U CN 201721880887 U CN201721880887 U CN 201721880887U CN 207729907 U CN207729907 U CN 207729907U
- Authority
- CN
- China
- Prior art keywords
- oxygen
- liquid
- tower
- nitrogen
- condenser
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a kind of equipment producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification, can meet the needs of market is to nitrogen and oxygen simultaneously, while ensureing yield, and can realize the requirement to nitrogen oxygen purity.The utility model has fully considered various aspects factor to realize steady, efficient, low energy consumption the operation of production High Purity Nitrogen, oxygen and liquid oxygen plant.
Description
Technical field
Equipment the utility model is related to produce High Purity Nitrogen, oxygen and liquid oxygen by cryogenic rectification.
Background technology
Mixture containing nitrogen and oxygen, most commonly air can be separated into rich nitrogen through cryogenic rectification and oxygen-enriched evaporate
Point and the fraction comprising rare gas, such as argon gas.In cryogenic rectification, by air purge, compression, to remove height boiling impurity
(such as carbon dioxide), water vapour and hydrocarbon.Then the air stream of the purifying of gained and compression is cooled to suitable for essence
The temperature evaporated.Rectifying generates rich nitrogen and oxygen-enriched fraction and other desired fraction, can be liquids and gases Product Form.
There are different rectifying columns arrangements for this purpose.
In recent years, in petrochemical industry, blast furnace ironmaking, the fields such as electronic industry are big to the demand of High Purity Nitrogen and high pure oxygen
It is big to increase.Therefore efficient, energy saving, the method and apparatus of the production High Purity Nitrogen and high pure oxygen cut down expenses is needed.
Chinese utility model patent CN202648307U describes a kind of equipment detaching air by cryogenic rectification, profit
The condenser for being arranged in tower top with two can generate High Purity Nitrogen in a destilling tower.But height can only be produced in the utility model
Purity nitrogen and high pure oxygen cannot be produced, cannot be satisfied the demand for high pure oxygen, do not have general applicability.
Utility model content
Technical problem to be solved in the utility model is the production how under the premise of the production of High Purity Nitrogen is unaffected
High pure oxygen and oxygen are produced while High Purity Nitrogen.
To solve the above-mentioned problems, the utility model discloses one kind by cryogenic rectification produced from air High Purity Nitrogen,
The equipment of oxygen and liquid oxygen, the equipment include：
By raw air compression, the equipment of purifying and the logistics that generates itself and cryogenic rectification carry out indirect heat exchange with the
The second main heat exchanger the first connected main heat exchanger of one destilling tower and be connected with after-fractionating tower.
Including several distillation sections, compressed, purifying, the first cooling raw air are provided to the first distillation section, it will
It is separated into the first destilling tower in the first oxygen enriched liquid of first nitrogen rich vapor and bottom of tower on top.
So that the first nitrogen rich vapor of first part and the first oxygen enriched liquid of first part is carried out indirect heat exchange, makes first part
The condensation of first nitrogen rich vapor generates first part's richness nitrogen condensate liquid, and the first oxygen enriched liquid of first part is made at least partly to gasify, raw
At the first condenser of the second nitrogen rich vapor and hyperoxia quantity of fluid.
So that at least part of hyperoxia quantity of fluid is carried out indirect heat exchange with the first nitrogen rich vapor of second part, makes second part
The condensation of first nitrogen rich vapor generates second part richness nitrogen condensate liquid, and the hyperoxia quantity of fluid is made at least partly to gasify, and generates first
Second condenser of waste stream.
To send at least partly rich nitrogen condensate liquid back to first destilling tower as the equipment of phegma.
To the first compressor for compressing the second nitrogen rich vapor, to cooling first circulation stream, and by first circulation stream
Send to the equipment of the after-fractionating section of the first destilling tower, wherein after-fractionating section be located at first distillation section below and
Every at least one theoretical cam curve.
Remaining hyperoxia quantity of fluid is as the expanded feeding second afterwards of the second oxygen enriched liquid after being vaporized in second condenser
The pipeline and expansion valve of destilling tower.
After-fractionating tower, after-fractionating tower upper space, after-fractionating tower distill section, after-fractionating tower lower space and
For the after-fractionating tower reboiler of reboiling liquid oxygen.
The second main heat exchanger re-heat is inputted from after-fractionating tower upper space by the second waste stream, and through the second compressor
Defeated time the second main heat exchanger cooling again after compression, then input the pipeline of after-fractionating tower lower space.
Pressurized, purifying the second raw air is inputted into the cooling of the second main heat exchanger, then is inputted under after-fractionating tower
The pipeline in portion space.
Oxygen deprivation steam in after-fractionating tower lower space is conveyed into the pipeline of after-fractionating tower reboiler, and will condensation
Oxygen deprivation liquid afterwards is transmitted back to the pipeline of after-fractionating tower lower space.
The second main heat is conveyed into after the second liquid oxygen in after-fractionating tower reboiler is pressurized alternatively through liquid oxygen pump to hand over
Parallel operation re-heat, and as the pipeline of the second oxygen product output.
Oxygen deprivation liquid in after-fractionating tower lower space (43) is conveyed into the pipe of after-fractionating tower upper space respectively
Road and the pipeline converged with the first oxygen enriched liquid.
In the first destilling tower, above the first distillation section and the third of at least one theoretical cam curve in interval is distilled
Section, a part for phegma is extracted from third distillation section, and the liquid air as no high boiling component conveys after expansion valve
Enter the equipment at the top of third destilling tower.
Positioned at the third destilling tower reboiler of third destilling tower lower space, wherein after expansion without high boiling component
Liquid portion in liquid air flows through the distillation section of third destilling tower, herein with the second part that is introduced from the first destilling tower
One oxygen enriched liquid indirect heat exchange, and third liquid oxygen product is generated in the bottom of third destilling tower, second part after cooling the
One oxygen enriched liquid is transmitted back to first or second condenser.
The third waste stream that will be generated at the top of third destilling tower optionally after merging with the first waste stream, is sent to
The equipment of one main heat exchanger and the first raw air indirect heat exchange.
At least partly described first waste stream and/or first raw air are expanded and provided for cryogenic rectification process
The expanding machine of required cold.
Wherein, first compressor and expanding machine are mechanically coupled.
Wherein, the first condenser, the second condenser and reboiler are made of plate heat exchanger in above equipment.
Using the equipment of production High Purity Nitrogen disclosed by the utility model, oxygen and liquid oxygen, market can be met simultaneously to nitrogen
With the demand of oxygen, while ensureing yield, and the requirement to nitrogen oxygen purity can be realized.The utility model has fully considered each side
Face factor is to realize steady, efficient, low energy consumption the operation of production High Purity Nitrogen, oxygen and liquid oxygen plant.
Description of the drawings
Attached drawing in the utility model is only as the signal to the utility model, for understanding and explaining the essence of the utility model
God, but the utility model is not limited in any way.
Fig. 1 is the schematic diagram of the utility model one embodiment.
Specific implementation mode
In the present invention, term " raw air " means the mixture for mainly including oxygen and nitrogen.Term " theoretical tower
Plate " means that air-liquid two-phase is all sufficiently mixed on it, and heat transfer and mass transport process resistance are 0 idealization column plate." distillation
Section " refers to having certain intervals in destilling tower mutually, and each section all includes the structure of several rectifiying plates.
With reference to attached drawing.It first passes around a series of widely-known techniques dryings and purifies raw air 101, the technology can
Including filter, temperature swing adsorbers etc..Such as raw air is made to remove the solid impurities such as dust by filter, using molecule
It sieves clarifier or temperature swing adsorbers removes the foreign gases such as vapor and carbon dioxide.At least part of the subsequent raw air
It can be compressed to the pressure close or equal with the operating pressure of the first destilling tower through main air compressor and be conveyed into the first main heat
Exchanger 1.
First raw air 101 low temperature logistics generated in the process that are distillated in the first main heat exchanger 1 are cooled to one
As less than -150 DEG C and be transported to the first destilling tower 2 first distillation section 8, in the first destilling tower 2, cooled first
Raw air passes sequentially through the first distillation section 8, and third distills section 7, and is connect for the phegma adverse current of liquid nitrogen with main component
It touches.Therefore, the oxygen in gas phase and the boiling point component (methane, krypton, xenon etc.) higher than oxygen are dissolved in phegma, and in liquid phase
In nitrogen and the boiling point component (neon, hydrogen, helium etc.) lower than nitrogen be evaporated and be released into gas phase.As a result, in distillation section
Top formed the first nitrogen rich vapor 105 and 114, the first destilling tower 2 bottom of tower formation the first oxygen enriched liquid 103 and 135.The
A part of first oxygen enriched liquid 103 can be transported to the first condenser 3 of the first destilling tower 2 after throttle valve expands.
The first nitrogen rich vapor of first part 105 at the top of distillation section is via Pipeline transport to the first condenser unit
In 4, by be transported to the first oxygen enriched liquid of first part 103 after the expansion of the first condenser 3 and carry out indirect heat exchange
And be condensed, first part's richness nitrogen condensate liquid 111 is generated, first part's richness nitrogen condensate liquid can return to the distillation of the first destilling tower 2
It is taken out via pipeline portions as phegma or as liquid nitrogen product 112 at the top of section.
In the first condenser 3, due to indirect heat exchange, the first oxygen enriched liquid 103 at least partly gasifies, in the first condensation
The steam phase of the hyperoxia quantity of fluid 113 and rich nitrogen of liquid phase, i.e. the second nitrogen rich vapor 125 are generated in the shell of device 3.Hyperoxia quantity of fluid
113 are transported to the second condenser 5 upon inflation.Second nitrogen rich vapor has higher oxygen content, oxygen compared with raw air
Content is generally in 25~29 mole percents.
The first nitrogen rich vapor of second part 114 at the top of distillation section is via Pipeline transport to the second condenser unit
6, it is condensed by carrying out indirect heat exchange with the hyperoxia quantity of fluid 113 for being transported to the second condenser 5, generates second part
Rich nitrogen condensate liquid 115, second part richness nitrogen condensate liquid can return to the top of the distillation section of the first destilling tower 2 as phegma or
It is taken out via pipeline portions as liquid nitrogen product 112.
Hyperoxia quantity of fluid in second condenser 5 at least partly gasifies by indirect heat exchange, generates the first waste stream 121,
Pass through the heating of the first main heat exchanger 1 respectively and expanding machine 30 expand, and in the first main heat exchanger 1 with raw air into one
Indirect heat exchange is walked, is further heated up and is discharged as waste gas stream.Oxygen content in first waste stream is generally higher than 46 Mole percents
Number.
At least partly the second nitrogen rich vapor 125 formed in the first condenser 3 is formed first through the first compressor 31
The first circulation stream 132 cooled down by the first main heat exchanger 1 is transported to the after-fractionating of the first destilling tower 2 by recycle stream 131
Section 9.Wherein, after-fractionating section 9 is located at 8 lower section of the first distillation section and at least one theoretical cam curve in interval.
In the preferred embodiment of the utility model, expanding machine 30 and the first compressor 31 be it is mechanically connected connect,
Therefore the part energy released when gas expansion can be used directly for compression.Simultaneously as liquids in the first condenser 3
Stream is discharged so that containing less oxygen in the logistics of evaporation, and the first condenser 3 can maintain higher pressure, to make this
Gas required work in compressor compresses lowers, and can have high flow when the input work of isodose gives the first compressor 31
Recirculation flow.The high flow capacity of recirculation flow makes the first destilling tower 2 have high nitrogen recovery with high nitrogen concentration.
Optionally, at least partly the first nitrogen rich vapor 105 and 114 can be taken off as nitrogen product 151.
The second oxygen enriched liquid 160 is extracted in remaining hyperoxia quantity of fluid 113 after being vaporized in the second condenser 5, it is expanded
It is sent into after-fractionating tower 40 afterwards, the second oxygen enriched liquid 160 after expansion includes the gentle body portion of liquid portion, the liquid portion
The after-fractionating tower reboiler 44 positioned at 40 lower part of after-fractionating tower is flowed down to, the gas part rises and given birth at top
At the second waste stream 164, after which flows through 33 re-heat of the second main heat exchanger, at least partly pressed through the second compressor 32
Second circulation stream 165 is generated after contracting, in the second main heat exchanger 33, second circulation stream 165 with it is compressed after purification second
Raw air 161 can input after-fractionating tower with high pressure liquid oxygen 174 and 164 indirect heat exchange of the second waste stream and after cooling down
Lower space 43.
After-fractionating tower lower space 43 contains oxygen deprivation steam and oxygen deprivation liquid, and at least partly oxygen deprivation steam 166 is as warm
Source is conveyed into after-fractionating tower reboiler 44, and the second oxygen enriched liquid indirect heat exchange after rectifying, and at least partly condenses
It generates oxygen deprivation liquid 167 and returns to after-fractionating tower lower space 43.Extract remaining second liquid in after-fractionating tower reboiler 44
Oxygen 173 can export after re-heat as the second oxygen product 175 after the supercharging of liquid oxygen pump 34 in the second main heat exchanger 33.
It extracts the oxygen deprivation liquid in after-fractionating tower lower space 43 and is divided at least two parts, first part's oxygen deprivation liquid
162 it is expanded after be introduced into after-fractionating tower upper space 41 be used as phegma, can after second part oxygen deprivation liquid 163 is expanded
It is mixed with 135 with the first oxygen enriched liquid 103 and is admitted to the first condenser 3.
The part that phegma is extracted from third distillation section 7, the liquid air 133 as no high boiling component are expanded rear defeated
It is sent to the top of third destilling tower 20.Wherein, third distills section 7 and is located at 8 top of the first distillation section and is spaced at least
One theoretical cam curve.
The liquid air without high boiling component after expansion includes the gentle body portion of liquid portion, in third destilling tower upper space
The gas part of 21 portion collection gas-liquid mixtures, liquid portion distill column distillation as phegma down through third
Section 22, liquid releases low boiling component to improve the oxygen content of liquid in the section.In third destilling tower lower part
The third destilling tower reboiler 24 that liquid is collected for heating lower space is installed, in third destilling tower reboiler in space 23
Liquid portion and 135 indirect heat exchange of the first oxygen enriched liquid of second part introduced from the first destilling tower 2 in 24, than oxygen boiling point
Low component (argon, carbon dioxide, nitrogen etc.) rises through third destilling tower distillation section 22 by selective evaporation.Finally
Nitrogen containing the low boiling component than oxygen low boiling point is collected in third destilling tower upper space 21, distills tower bottom in third
Ultra-high purity liquid oxygen is generated, i.e. third liquid oxygen product 145, the first oxygen enriched liquid of second part after cooling is transmitted back to the 1st
Or second condenser 5.
Third waste stream 143 is collected in third destilling tower upper space 21 (containing the low boiling point group than oxygen low boiling point
Point), through demi-inflation, optionally, merge with the first expanded waste stream, in the first main heat exchanger 1 with the first raw material
Air indirect heat exchange is further heated up as waste gas stream.
In third destilling tower reboiler 24, heat source is that the second part first that 2 bottom of tower of the first destilling tower is formed is oxygen-enriched
Liquid 135 is cooled into third destilling tower reboiler 24 after carrying out indirect heat exchange with first oxygen enriched liquid 135,
The first oxygen enriched liquid of second part 141 after cooling is transmitted back to first or second condenser after demi-inflation.
Wherein, at least partly described first waste stream and/or first raw air expand in expanding machine, are
The above process provides required cold.
Embodiment：
According to the utility model proposes technique, manufactured the process units of a nitrogen, it produce nitrogen oxygen content do not surpass
1ppm is crossed, the air pressure of product nitrogen output is 9.5bar, flow 10000Nm3/h；The production dress of a high pure oxygen is also manufactured
It sets, the oxygen amount containing argon that it is produced is no more than 100ppb, and the pressure of high pure oxygen product output is 1.5bar, flow 129Nm3/h。
The process units of an oxygen has also been manufactured simultaneously, and the air pressure of product oxygen output is 7.5bar, flow 315Nm3/ h, and contain body
The argon that fraction is 0.5%.
20 DEG C, 9.8bar, 19740Nm3The drying of/h and (the actually anhydrous and CO of pure air stream 1012) into first
Before first distillation section 8 of destilling tower 2, initially enters the first main heat exchanger 1 and be cooled to -164.3 DEG C.
Oxygen content is 38.2 mole percents, flow 15850Nm3First part's oxygen enriched liquid 103 of/h is steamed from first
Evaporate the bottom discharge of tower 2, the first oxygen enriched liquid of first part 103 of 35.6% volume fraction is transported to the after throttle valve expands
First condenser 3 of one destilling tower 2, the first oxygen enriched liquid of second part 135 for being left 64.4% volume fraction are used as heat source quilt
Be transported to third destilling tower reboiler 24, be transmitted back to after the first oxygen enriched liquid 141 after cooling is expanded first condenser 3 or
Second condenser 5.
Oxygen content is 26.8 mole percents, flow 7980Nm3The second nitrogen rich vapor 125 of/h -171.2 DEG C,
6.0bar is exported by the first condenser 3, the second nitrogen rich vapor 125 first after the first compressor 31 is compressed to 9.8bar, using
First main heat exchanger 1 cools down and is transported to the after-fractionating section 9 of the first destilling tower 2.
The hyperoxia quantity of fluid 113 for the surplus being sent into the first condenser 3 by being sent into after expansion in the second condenser 5,
4.7bar, -171.2 DEG C of gasifications.
Gaseous first waste stream 121 is sent into the first main heat exchanger 1 and is warming up to -140.7 DEG C, then in expanding machine
After 30 expansions, it can merge with the third waste stream 143 that 20 top of third destilling tower generates, reenter the first main heat exchanger 1,
It is warming up to 18 DEG C herein.The waste stream is with 9660Nm3The flow of/h is discharged, and oxygen content therein is 39.1 mole percents.
- 170.0 DEG C, 9.7bar, 10000Nm being discharged by 2 top of the first destilling tower3The first nitrogen rich vapor 151 of/h,
It is transferred out using 9.5bar as High Purity Nitrogen product after being warming up to 18 DEG C in first main heat exchanger 1.
From the third of the first destilling tower 2 distillation section 7 extract -168.3 DEG C without high boiling component, 9.7bar,
1890Nm3/ h, the liquid air 133 without high boiling component that oxygen content is 11.6 mole percents, are conveyed into third after expansion
The upper space of destilling tower 20.
- 178.7 DEG C, 1.5bar, 129Nm are extracted in the bottom of third destilling tower 203High-purity oxygen liquid of/h and as
Three liquid oxygen products 145 export.Third waste stream 143 is generated in the upper space of third destilling tower 20, optionally, with the first waste
Stream 121 merges.
- 171.2 DEG C, 4.7bar, 448Nm are extracted in remaining hyperoxia quantity of fluid 113 after being vaporized in the second condenser 53/
H, oxygen content is the second oxygen-enriched liquid 160 of 70.0 mole percents, and after-fractionating tower 40 is sent into after expanded.
- 181.4 DEG C, 3.1bar, 1060Nm are generated at the top of after-fractionating tower 403/ h, oxygen content are 14.3 mole hundred
Second waste stream 164 of score, second waste stream 164 flow through the second main heat exchanger 33 and are warming up to 18 DEG C, 91.7% volume
Second waste stream of score is compressed to 9.7bar by the second compressor 32, after by the second main heat exchanger 33 be input to second
Destilling tower lower space 43；Second waste stream of remaining 8.3% volume fraction is discharged after purifying and expanding as exhaust gas.
20 DEG C, 20.9bar, 435Nm3The drying of/h and pure high pressure air flow 161, initially enter the second main heat exchanger
33 are cooled to -163.5 DEG C, after be input to after-fractionating tower lower space 43.
1410Nm is extracted in after-fractionating tower lower space 433/ h, the oxygen deprivation liquid that oxygen content is 16.4 mole percents
Body.It is introduced into 41 conduct of after-fractionating tower upper space after first part's oxygen deprivation liquid 162 of 65.9% volume fraction is expanded
Phegma, can be with the first oxygen-rich liquid of first part after the second part oxygen deprivation liquid 163 of remaining 34.1% volume fraction is expanded
Body 103 mixes and is admitted to the first condenser 3.
Extract -170.6 DEG C, 3.1bar, 315Nm in after-fractionating tower reboiler 443The second liquid oxygen 173 of/h, can be through liquid
Oxygen pump 34 boosts to 7.7bar, defeated using 18 DEG C, 7.5bar as the second oxygen product after the heating of the second main heat exchanger 33
Go out.
Claims (3)
1. a kind of equipment producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification, including：
(a) by raw air compression, the equipment of purifying and the logistics that generates itself and cryogenic rectification carry out indirect heat exchange with the
The second main heat exchanger (33) one destilling tower (2) connected the first main heat exchanger (1) and be connected with after-fractionating tower (40)；
(b) the first destilling tower (2) provide compressed, purifying, cooling including several distillation sections to the first distillation section (8)
First raw air (101) is separated into first nitrogen rich vapor (105,114) on top and the first oxygen enriched liquid of bottom of tower
(103,135)；
(c) the first condenser (3), wherein the first oxygen enriched liquid of the first nitrogen rich vapor of first part (105) and first part
(103) in the first condenser (3) indirect heat exchange, the first nitrogen rich vapor of first part (105) condensation is made to generate first part rich
Nitrogen condensate liquid (111) makes the first oxygen enriched liquid of the first part (103) at least partly vaporize, and generates the second nitrogen rich vapor
(125) and hyperoxia quantity of fluid (113)；
(d) the second condenser (5), wherein at least part of hyperoxia quantity of fluid (113) and the first nitrogen rich vapor of second part
(114) indirect heat exchange is carried out in the second condenser (5), the first nitrogen rich vapor of second part (114) condensation is made to generate second
Separation nitrogen-enriching condensate liquid (115) makes the hyperoxia quantity of fluid (113) at least partly vaporize, and generates the first waste stream (121)；
(e) sending at least partly rich nitrogen condensate liquid (111,115) equipment of the first destilling tower (2) as phegma back to；
(f) cooling simultaneously as first circulation stream (131) to compress the second nitrogen rich vapor (125) through the first compressor (31)
It send to the equipment of the after-fractionating section (9) of the first destilling tower (2), wherein after-fractionating section (9) is located at the first distillation section
(8) at least one theoretical cam curve in lower section and interval；
(g) it is used as the second oxygen enriched liquid (160) through swollen remaining hyperoxia quantity of fluid (113) after vaporization in second condenser (5)
The pipeline and expansion valve of after-fractionating tower (40) are sent into after swollen；
(h) after-fractionating tower (40), after-fractionating tower upper space (41), after-fractionating tower distill section (42), after-fractionating
Tower lower space (43) and after-fractionating tower reboiler (44) for reboiling liquid oxygen；
(i) the second main heat exchanger (33) re-heat is inputted from after-fractionating tower upper space (41) by the second waste stream (164), and
Defeated time the second main heat exchanger (33) is cooling again after the second compressor (32) compression, then inputs after-fractionating tower lower space
(43) pipeline；
(j) pressurized, purifying the second raw air (161) is inputted into the second main heat exchanger (33) cooling, then inputs second
The pipeline of destilling tower lower space (43)；
(k) the oxygen deprivation steam (166) in after-fractionating tower lower space (43) is conveyed into after-fractionating tower reboiler (44)
Pipeline, and condensed oxygen deprivation liquid (167) is transmitted back to the pipeline of after-fractionating tower lower space (43)；
(l) it is conveyed after being pressurized the second liquid oxygen (173) in after-fractionating tower reboiler (44) alternatively through liquid oxygen pump (34)
Enter the second main heat exchanger (33) re-heat, and as the pipeline of the second oxygen product output；
(m) the oxygen deprivation liquid in after-fractionating tower lower space (43) is conveyed into after-fractionating tower upper space (41) respectively
Pipeline (162) and the pipeline (163) converged with the first oxygen enriched liquid；
(n) be located in the first destilling tower (2), above the first distillation section (8) and at least one theoretical cam curve in interval the
Three distillation sections (7), a part for phegma, the liquid air as no high boiling component are extracted from third distillation section (7)
(133) equipment that the top of third destilling tower (20) is conveyed into after expanded；
(o) be located at third destilling tower (20) lower space third destilling tower reboiler (24), wherein after expansion without higher boiling
Liquid portion in the liquid air of component flows through the distillation section (22) of third destilling tower (20), draws herein with from the first destilling tower
The first oxygen enriched liquid of second part (135) indirect heat exchange entered, and generate third liquid oxygen in the bottom of third destilling tower (20)
Product (145), the first oxygen enriched liquid of second part (141) after cooling are transmitted back to the first condenser (3) or the second condenser
(5)；
(p) the third waste stream (143) that will be generated at the top of third destilling tower (20), optionally, with the first waste stream (121)
After merging, send to the equipment of the first main heat exchanger (1) and the first raw air (101) indirect heat exchange；
(q) at least partly described first waste stream (121) and/or first raw air are expanded and are by expanding machine (30)
Cryogenic rectification process provides required cold.
2. equipment as described in claim 1, wherein first compressor (31) and expanding machine (30) is mechanical communication
's.
3. equipment as claimed in claim 1 or 2, wherein the first condenser (3), the second condenser (5) and reboiler (24,
44) it is made of plate heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721880887.3U CN207729907U (en) | 2017-12-28 | 2017-12-28 | The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721880887.3U CN207729907U (en) | 2017-12-28 | 2017-12-28 | The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207729907U true CN207729907U (en) | 2018-08-14 |
Family
ID=63087318
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721880887.3U Expired - Fee Related CN207729907U (en) | 2017-12-28 | 2017-12-28 | The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207729907U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036584A (en) * | 2017-12-28 | 2018-05-15 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification |
-
2017
- 2017-12-28 CN CN201721880887.3U patent/CN207729907U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036584A (en) * | 2017-12-28 | 2018-05-15 | 乔治洛德方法研究和开发液化空气有限公司 | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4331460B2 (en) | Method and apparatus for producing krypton and / or xenon by low temperature air separation | |
| CN103123203B (en) | Method of preparing pure nitrogen by using exhaust gas with nitrogen to carry out once-more cryogenic distillation | |
| CN1239877C (en) | Low-temperature air-separating three-tower system | |
| JPH08210769A (en) | Cryogenic rectification system with side column for forming low-purity oxygen | |
| JPH0140271B2 (en) | ||
| JPH0571870A (en) | Method and device for manufacturing high pressure nitrogen | |
| JPH0719727A (en) | Separation of air | |
| JPH0735470A (en) | Method and device for manufacturing superhigh purity dinitrogen monoxide | |
| TW200403420A (en) | Air fractionation process and installation with mixing column and krypton-xenon recovery | |
| CN104990366B (en) | A kind of method that thick neon helium product is extracted in the liquid nitrogen from air separation unit | |
| JPH05203347A (en) | Extremely low temperature refining system for generation of highly pure oxygen | |
| JPH0731004B2 (en) | Air distillation method and plant | |
| KR960010365B1 (en) | Inter-column heat integration for multi-column distillation system | |
| JP4308432B2 (en) | Method and apparatus for producing nitrogen by low temperature distillation using a dephlegmator | |
| JPH05296651A (en) | Apparatus for producing nitrogen/oxygen of ultrahigh purity | |
| JPH05187765A (en) | Method and device for manufacturing ultrahigh purity nitrogen | |
| JP3545629B2 (en) | Cryogenic purification method and apparatus for producing ultra-high purity nitrogen and ultra-high purity oxygen | |
| JPH0661402B2 (en) | Multi-column distillation method with inter-column thermal coupling | |
| JPH0914832A (en) | Method and equipment for manufacturing ultra-high purity oxygen | |
| CN108036584A (en) | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification | |
| JPS6298184A (en) | Manufacture of krypton-xenon concentrate containing no oxygen | |
| JP2007064617A (en) | Method of manufacturing krypton and/or xenon by cryogenic air separation | |
| CN207729907U (en) | The equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification | |
| KR101238063B1 (en) | Nitrogen generating device and apparatus for use therefor | |
| CN207702828U (en) | The equipment for producing High Purity Nitrogen and oxygen from air by cryogenic rectification |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20180814 Termination date: 20181228 |