CN204513906U - A kind of empty point fractionating column system - Google Patents
A kind of empty point fractionating column system Download PDFInfo
- Publication number
- CN204513906U CN204513906U CN201520139001.4U CN201520139001U CN204513906U CN 204513906 U CN204513906 U CN 204513906U CN 201520139001 U CN201520139001 U CN 201520139001U CN 204513906 U CN204513906 U CN 204513906U
- Authority
- CN
- China
- Prior art keywords
- fractionating column
- tower
- evaporator
- condenser
- under
- 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 empty point fractionating column system, comprise the fractionating column be made up of tower under tower, condenser/evaporator and fractionating column on fractionating column, condenser/evaporator top is communicated with tower bottom on fractionating column, be connected with top of tower under fractionating column bottom condenser/evaporator, pressure air conduit connects tower under main heat exchanger, liquid oxygen evaporator and fractionating column in turn, and under fractionating column, tower bottom outlet connects tower on fractionating column by subcooler; Under fractionating column, tower first exports and is connected with condenser/evaporator, and condenser/evaporator first exports and connects tower on fractionating column by subcooler on the one hand, on the other hand tower under connection fractionating column; Condenser/evaporator outlet at bottom is connected with main heat exchanger by liquid oxygen evaporator, and on fractionating column, top of tower outlet is connected with main heat exchanger by subcooler, and on fractionating column, tower bottom outlet connects main heat exchanger.The utility model system can produce lower purity oxygen and the high pure nitrogen of two kinds of different purity and pressure simultaneously, and operating pressure is low, and recovery rate is high, less energy consumption, and equipment investment is low.
Description
Technical field
The utility model belongs to air-separating plant technical field, is specifically related to a kind of empty point fractionating column system.
Background technology
Along with the emergence of the industries such as China's Coal Chemical Industry, petrochemical industry, integrated gasification combined cycle for power generation system (IGCC), nonferrous smelting, many new demands are proposed to air separation plant.Safe and reliable, energy-saving and emission-reduction, this is basic demand to air separation plant and precondition, is to build a resource-conserving and environment-friendly society and the needs of scientific development, is also the common expectation of air separation plant user.Because technical development is maked rapid progress, the relation of empty point industry and these industries has not been the relation of simple supply and demand, but mutually incorporate technically and combine, empty point flow process combines with user's technique, reaches optimization, raises the efficiency, exploit potentialities, energy-saving and cost-reducing, increase economic efficiency, realize supply and demand doulbe-sides' victory.
The oxygen purity that current typical air separation plant is produced is about 99.6%, and the operating pressure of lower tower is about 0.45 (G), and consider pipeline and lose along journey equipment resistance, air compressor machine pressure at expulsion is between 0.48 ~ 0.52MPa (G) scope; In order to meet the purity requirement of oxygen and nitrogen, upper tower number of theoretical plate is generally about 75 pieces.But the oxygen adopting purity 95% in nonferrous smelting, Coal Chemical Industry, the medium industry in IGCC power station more, the even oxygen of the lower 60%-85% of purity.For coordinating this oxygen feature, on conventional deep-cooling space division technique basis, reduce air compressor machine row pressure, in minimizing, tower height degree, arranges liquid oxygen evaporator simultaneously, increases oxygen and goes out pressure tower, develop a kind of novel low purity oxygen preparation system.
Integrated gasification combined cycle plants (IGCC, Integrated Gasification Combined Cycle) electricity generation system, be advanced power systems Coal Gasification Technology and efficient combined cycle technique combined, IGCC generation technology is current one of the most noticeable novel, efficient Clean Coal Power Generating Technologies in the world.In IGCC electricity generation system, oxygen plays critical effect as gasifying agent to the raising efficiency of carbon con version of gasification furnace and the single-machine capacity in IGCC power station.Because IGCC oxygen demand is large, the exploration of air separation plant power-saving technology becomes the important topic improving IGCC whole efficiency further.At present, in IGCC power station, most gasification furnace adopts the oxygen of purity 95%, also has some to adopt purity to be the oxygen of 85%.In theory, various gasification furnace all can adopt purity to be about 85% even lower oxygen, and most of gasification furnace adopts the oxygen of purity >=95%, mainly in order to mate with current conventional oxygen from air separation plant purity (99.6%).
Coal chemical industry: coal gasification, coal liquifaction, olefin hydrocarbon making by coal etc., all only need 90%-95%O
2the oxygen of purity.
Metallurgy industry: rich-oxygen of blast furnace is smelted iron, as long as oxygen content, than oxygen content height 3%-5% in air, therefore uses 90%O in air blast
2the oxygen of left and right purity mixes in air blast.Molten blast furnace reduction (COREX) method ironmaking and copper flash smelting furnace, all can by purity at 70%-90%O
2the left and right oxygen that even purity is lower.
The high purity oxygen (99.6%) that conventional Deep Cooling Method air separation plant is produced is diluted to low purity oxygen uneconomical, and can produces low purity oxygen and energy-conservation THE PRESSURE SWING ADSORPTION OXYGEN GENERATING DEVICE oxygen yield is limited, floor space is large, can not produce nitrogen and fluid product again simultaneously.Therefore, a kind of Deep Cooling Method air separation plant of safe and reliable, energy-saving and cost-reducing maximization low-purity oxygen more can meet the demands.
Utility model content
The purpose of this utility model is to provide a kind of empty point fractionating column system.
A kind of empty point fractionating column system, comprise the fractionating column be made up of tower under tower, condenser/evaporator and fractionating column on fractionating column, condenser/evaporator top is communicated with tower bottom on fractionating column, be connected with top of tower under fractionating column bottom condenser/evaporator, pressure air conduit connects tower under main heat exchanger, liquid oxygen evaporator and fractionating column in turn, and under fractionating column, tower bottom outlet connects tower on fractionating column by subcooler; Under fractionating column, tower first exports and is connected with condenser/evaporator, and condenser/evaporator first exports and connects tower on fractionating column by subcooler on the one hand, on the other hand tower under connection fractionating column; Condenser/evaporator outlet at bottom is connected with main heat exchanger by liquid oxygen evaporator, and on fractionating column, top of tower outlet is connected with main heat exchanger by subcooler, and on fractionating column, tower bottom outlet connects main heat exchanger.
Under described fractionating column, tower is packed tower or sieve-plate tower.On fractionating column, the tower number of plates is 35-54 block, and on fractionating column, tower and ice chest reduce at a high speed thereupon, and equipment investment reduces; Under fractionating column, tower bottom outlet connects tower 13-18 block column plate place on fractionating column by subcooler.
In order to make nitrogen gas purity higher (> 99%), on fractionating column, the 6-9 column plate place of tower is provided with dirty nitrogen outlet, and dirty nitrogen outlet is connected with main heat exchanger by subcooler.
The position of liquid oxygen evaporator, lower than condenser/evaporator, makes the fluid column static pressure supercharging that low pure liquid oxygen utilizes self gravitation to produce.
Utilize above-mentioned sky to divide fractionating column system to prepare the technique of low purity oxygen, comprise the following steps:
(1) product that backflowed in main heat exchanger of the pressure air after cooling and purifying is cooled to saturation temperature, and then in liquid oxygen evaporator with after low pure liquid oxygen heat exchange, become the air of partial liquefaction, under then sending into fractionating column, rectifying participated in by tower;
(2) air of partial liquefaction is separated into the nitrogen of top of tower under the oxygen-enriched liquid air of tower bottom under fractionating column and fractionating column under fractionating column in tower, and oxygen-enriched liquid air sends into tower middle and upper part on fractionating column through subcooler; Nitrogen is cooled to liquid nitrogen in condenser/evaporator with after the liquid oxygen heat exchange of tower bottom on fractionating column, and a part of liquid nitrogen sends into tower on fractionating column by subcooler; Under another part sends fractionating column back to, top of tower is as phegma;
(3) each material (oxygen-enriched liquid air, liquid nitrogen and unclassified stores) entering tower on fractionating column is separated into the high pure nitrogen of top of tower on low pure liquid oxygen in condenser/evaporator and fractionating column, after low pure liquid oxygen gasifies with the nitrogen heat exchange of top of tower under fractionating column on the one hand in condenser/evaporator, tower bottom outlet on fractionating column, then send as product A after main heat exchanger re-heat to normal temperature; Send as product B after liquid oxygen evaporator, main heat exchanger heat exchange to normal temperature on the other hand.
According to the bubble point of tower bottom liquid oxygen on fractionating column in said method step (1), condenser/evaporator gets convenient temperature difference (those skilled in the art can operate according to the actual requirements), obtain the dew point of top of tower nitrogen under the fractionating column of heat exchange with it, thus the operating pressure of top of tower under determining fractionating column.
In said method step (1), under fractionating column, tower can be packed tower or sieve-plate tower, according to the turriform formula of tower under fractionating column, determine the operating pressure of tower bottom under fractionating column, then according to the pressure at expulsion of air compressor machine in the operating pressure of top of tower under fractionating column and bottom and the required resistance determination prior art of Air flow purification.
In said method, the pressure that product B can reach is determined by the heat transfer temperature difference of the dew point of the pressure air as its thermal source, the dew point of product B and liquid oxygen evaporator, low pure liquid oxygen reaches new balancing each other in liquid oxygen evaporator, its bottom liquid oxygen purity increases, so apparatus of the present invention can obtain highly purified oxygen and liquid oxygen by being arranged in series multiple liquid oxygen evaporator.
The utility model design is compared with conventional art and is had the following advantages:
(1) oxygen purity reduces and can reduce column bottom temperature on fractionating column, when the main cold temperature difference is constant, under fractionating column, top of tower temperature, pressure can synchronously reduce, air compressor machine pressure also can synchronously reduce, and the overwhelming majority of air compressor machine energy consumption duty separating device energy consumption, namely thus the overall energy consumption of air separation unit decline thereupon.
(2) the utility model arranges liquid oxygen evaporator, and position is lower than condenser/evaporator, and low pure liquid oxygen pressurizes through self fluid column static pressure after being extracted out by tower bottom on fractionating column, thus can obtain the product B of elevated pressures in liquid oxygen evaporator.
(3) the low pure liquid oxygen that tower bottom on fractionating column is extracted out is sent into liquid oxygen evaporator, re-establish wherein and balance each other, pressure air does thermal source, and flash distillation obtains the lower purity oxygen (product B) of higher degree, reduce further again air compressor machine pressure at expulsion simultaneously, reduce the overall energy consumption of air separation unit.
(4) because oxygen purity is lower, required upper tower rectifying theoretical cam curve reduces, thus upper tower height reduction, air separation unit ice chest also can reduce about 1/3rd, reduces equipment investment.
(5) can to separate pressure tower to 40KPa-80KPa(typical oxygen sky according to operating mode be about 15 KPa to the pressure of sending of product B), follow-up as needed compression, then before oxygen compressor machine, pressure improves, then press the energy consumption of oxygen system to decrease, and namely the overall energy consumption of air separation unit also can reduce.
(6) the utility model system requires depending on user the lower purity oxygen simultaneously can producing two kinds of different purity and pressure: on fractionating column, tower bottom evaporates the lower pressure (about 15KPa) of acquisition and the lower purity oxygen (product A) compared with low-purity by low pure liquid oxygen, the lower purity oxygen (product B) of the elevated pressures obtained in liquid oxygen evaporator (40KPa-80KPa) and higher degree.Also wherein any one can only be produced.
(7) air compressor machine pressure at expulsion reduces, thus air separation unit integrated operation pressure reduces, and recovery rate raises, and equipment investment reduces.According to differences such as unit scale, oxygen purity requirements, air separation unit air compressor machine pressure at expulsion can be low to moderate 0.28MPa (G)-0.45MPa (G), and oxygen extraction rate can to 95%-98%, and unit oxygen energy consumption can be low to moderate 0.27-0.36kwh/Nm
3o
2, equipment investment and conventional high-purity oxygen-air separation facility reduce about 12%-17%.
The utility model system can produce lower purity oxygen and the high pure nitrogen of two kinds of different purity and pressure simultaneously, operating pressure reduces, recovery rate is high, energy consumption reduces, equipment investment reduces, can be good at meeting the requirement to low-purity oxygen and high pure nitrogen such as coal chemical industry, nonferrous smelting, IGCC power station, be applicable to suitability for industrialized production.
Accompanying drawing explanation
Fig. 1 is the utility model sky point fractionating column system structural representation.
Detailed description of the invention
Below in conjunction with embodiment, the utility model is described further, but protection domain of the present utility model is not limited in this.
A kind of empty point fractionating column system, comprise the fractionating column be made up of tower 42 under tower on fractionating column 41, condenser/evaporator 6 and fractionating column, condenser/evaporator 6 top is communicated with bottom tower on fractionating column 41, bottom condenser/evaporator, 6 are connected with tower under fractionating column 42 top, pressure air conduit 1 connects tower 42 under main heat exchanger 2, liquid oxygen evaporator 3 and fractionating column in turn, and the number of plates that under fractionating column, tower 42 outlet at bottom connects tower 41 on tower 41(fractionating column on fractionating column by subcooler 5 is 48 pieces) 15-18 block column plate place, under fractionating column, the top first of tower 42 exports 8 and is connected with condenser/evaporator 6, condenser/evaporator 6 first exports 9 one aspects and connects tower 41 top on fractionating column by subcooler 5, the top of tower 42 under another aspect connection fractionating column, the outlet at bottom of condenser/evaporator 6 is connected with main heat exchanger 2 by liquid oxygen evaporator 3, on fractionating column, tower 41 top exit is connected with main heat exchanger 2 by subcooler 5, on fractionating column, tower 41 outlet at bottom connects main heat exchanger 2, on fractionating column, the 6-9 block column plate place of tower 41 is provided with dirty nitrogen outlet 7, dirty nitrogen outlet 7 is connected with main heat exchanger 2 by subcooler 5, under described fractionating column, tower 42 is sieve-plate tower, the position 4.6m lower than condenser/evaporator 6 of liquid oxygen evaporator 3.
The low purity oxygen utilizing said system to prepare 80% purity comprises the following steps:
(1) cooling and the pressure air after purifying are by pressure air conduit 1, backflowed after gas product is cooled to saturation temperature send into liquid oxygen evaporator 3 through main heat exchanger 2, and under sending into fractionating column as the air becoming partial liquefaction after thermal source heat exchange, rectifying participated in by tower 42;
(2) air of partial liquefaction is separated into the nitrogen at tower 42 top under oxygen-enriched liquid air under fractionating column bottom tower 42 and fractionating column under fractionating column in tower 42, and oxygen-enriched liquid air sends into the 15-18 block column plate place of tower 41 on fractionating column through subcooler 5; Nitrogen in condenser/evaporator 6 with condenser/evaporator 6 bottom liquid oxygen heat exchange after be cooled to liquid nitrogen, a part to be sent on fractionating column tower 41 top by subcooler 5 and is participated in rectifying; Under another part delivers to fractionating column, tower 42 top is as its phegma;
(3) each material (oxygen-enriched liquid air, liquid nitrogen and unclassified stores) entering tower 41 on fractionating column is separated into the high pure nitrogen at tower 41 top on 80% low pure liquid oxygen in condenser/evaporator 6 and fractionating column, 80% low pure liquid oxygen becomes the lower purity oxygen A of lower pressure (30KPa) and 53.5% purity on the one hand after gasifying with the nitrogen heat exchange at tower under fractionating column 42 top in condenser/evaporator 6, tower 41 outlet at bottom on fractionating column, then send as product A (purity 53.5%, pressure 15KPa) after main heat exchanger 2 re-heat to normal temperature; 80% low pure liquid oxygen sends into liquid oxygen evaporator 3 after the pressurization of self fluid column static pressure on the other hand, then sends as product B (purity 80%, pressure 57KPa) after main heat exchanger 2 heat exchange to normal temperature; Dirty nitrogen can obtain the nitrogen of purity > 99% after being discharged by dirty nitrogen outlet 7 from tower fractionating column 41 top, the nitrogen of purity > 99%, by subcooler 5, can utilize after heat exchange in main heat exchanger 2.
According to the bubble point of 80% low pure liquid oxygen, condenser/evaporator 6 gets the 0.6-1.5 DEG C of temperature difference, determine the pressure of the nitrogen of heat exchange with it, the i.e. operating pressure at tower 42 top under fractionating column, numerical value is 0.31MPa(G), again in conjunction with the resistance drop of the column plate resistance of tower under fractionating column 42, air precooling and purifying, can determine that air compressor machine pressure at expulsion is 0.37 MPa(G).
In above-mentioned technique, the pressure of product B is determined: the pressure air pressure as liquid oxygen evaporator 3 thermal source is: the resistance of air compressor machine pressure at expulsion-precooling purification system-through the resistance of main heat exchanger, be about 0.34MPa (G), after guarantee liquid oxygen evaporator 3 heat transfer temperature difference 0.7-1.6 DEG C, determine that wherein oxygen evaporating pressure is about 0.072MPa (G) i.e. 72KPa (G), determine that the lower purity oxygen purity obtained in liquid oxygen evaporator 3 is 80% thus, 72KPa (G), also can determine that its position is for 4.6m lower than condenser/evaporator 6 thus, sending an empty point ice chest gas product product B is 80%, 55KPa (G).
According to the method described in above-mentioned embodiment, the utility model can production purity simultaneously 53.5%, the product A of pressure 15KPa (G) and purity 80%, the product B of pressure 55KPa (G) and the high pure nitrogen of purity > 99%.Now air compressor machine pressure at expulsion is 0.37MPa (G), and the recovery rate of oxygen is 97%, and Unit consumption for oxygen production is 0.327kwh/Nm3O2, and equipment investment saves about 13%.
Claims (5)
1. a sky divides fractionating column system, it is characterized in that, comprise the fractionating column be made up of tower under tower, condenser/evaporator and fractionating column on fractionating column, condenser/evaporator top is communicated with tower bottom on fractionating column, be connected with top of tower under fractionating column bottom condenser/evaporator, pressure air conduit connects tower under main heat exchanger, liquid oxygen evaporator and fractionating column in turn, and under fractionating column, tower bottom outlet connects tower on fractionating column by subcooler; Under fractionating column, tower first exports and is connected with condenser/evaporator, and condenser/evaporator first exports and connects tower on fractionating column by subcooler on the one hand, on the other hand tower under connection fractionating column; Condenser/evaporator outlet at bottom is connected with main heat exchanger by liquid oxygen evaporator, and on fractionating column, top of tower outlet is connected with main heat exchanger by subcooler, and on fractionating column, tower bottom outlet connects main heat exchanger.
2. a kind of empty point fractionating column system as claimed in claim 1, it is characterized in that, under described fractionating column, tower is packed tower or sieve-plate tower.
3. a kind of empty point fractionating column system as claimed in claim 1, it is characterized in that, on fractionating column, the tower number of plates is 35-54 block; Under fractionating column, tower bottom outlet connects tower 13-18 block column plate place on fractionating column by subcooler.
4. a kind of empty point fractionating column system as claimed in claim 1, it is characterized in that, on fractionating column, the 6-9 column plate place of tower is provided with dirty nitrogen outlet, and dirty nitrogen outlet is connected with main heat exchanger by subcooler.
5. a kind of empty point fractionating column system as claimed in claim 1, it is characterized in that, the position of liquid oxygen evaporator is lower than condenser/evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520139001.4U CN204513906U (en) | 2015-03-12 | 2015-03-12 | A kind of empty point fractionating column system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520139001.4U CN204513906U (en) | 2015-03-12 | 2015-03-12 | A kind of empty point fractionating column system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204513906U true CN204513906U (en) | 2015-07-29 |
Family
ID=53711877
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520139001.4U Expired - Fee Related CN204513906U (en) | 2015-03-12 | 2015-03-12 | A kind of empty point fractionating column system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204513906U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI687633B (en) * | 2015-10-20 | 2020-03-11 | 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 | Oxygen production system and oxygen production method |
-
2015
- 2015-03-12 CN CN201520139001.4U patent/CN204513906U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI687633B (en) * | 2015-10-20 | 2020-03-11 | 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 | Oxygen production system and oxygen production method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104677052B (en) | Air separation fractionating tower system and technology utilizing air separation fractioning tower system to prepare low-purity oxygen | |
| CN102230716A (en) | Method and device for separating air through air pressurization, backflow expansion and internal compression | |
| CN105066587A (en) | Cryogenic separation and low-purity oxygen and high-purity oxygen and nitrogen production device and method | |
| CN203572141U (en) | Air separation system with regeneration air auxiliary rectification and depressurization functions | |
| CN102923714A (en) | Next-door thermal coupling distillation method and equipment for producing polycrystalline silicon | |
| CN110207460A (en) | A kind of recyclable device and its recovery method of integrated High Purity Nitrogen and argon gas | |
| CN2811892Y (en) | Air separator by back streaming expansion | |
| CN108645118A (en) | A kind of device and method improving the argon gas rate of recovery | |
| CN104964516A (en) | Partly-integrated type air separation device matched with IGCC power plant and method achieved through partly-integrated type air separation device | |
| CN101441023A (en) | Energy-saving type air separation process | |
| CN215412752U (en) | Double-tower low-temperature rectification high-purity nitrogen preparation device | |
| CN205373261U (en) | Low positive pressure of low high extraction percentage of liquid flows large -scale interior compression air separation system of inflation | |
| CN102141337A (en) | Method for separating air | |
| CN102809262B (en) | A kind of method and device utilizing IGCC gas turbine compressed air production oxygen | |
| CN108224900B (en) | Oxygen-nitrogen-argon separation system utilizing liquefied natural gas cold energy | |
| CN204513906U (en) | A kind of empty point fractionating column system | |
| Zhang et al. | A new heating system for the air pre-purification of air separation units | |
| CN202204239U (en) | Device for producing high-purity nitrogen and low-purity oxygen with pressure | |
| CN106871576B (en) | Commercial syngas low temperature front-end demethanization method and system | |
| CN205119656U (en) | Part wholeization type air separation plant in supporting IGCC power station | |
| CN109883139B (en) | Efficient argon extraction process based on oxygen-enriched air separation | |
| CN204718303U (en) | A kind of air-separating plant preparing pressure oxygen | |
| CN100443838C (en) | Method and equipment for separating stream backed expansion air | |
| JPH1163810A (en) | Method and device for manufacturing low purity oxygen | |
| CN203068914U (en) | High purity nitrogen production device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| 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: 20150729 Termination date: 20170312 |