CN102252500A - Method for utilizing oxygen-nitrogen liquefaction device to prepare high-purity oxygen - Google Patents
Method for utilizing oxygen-nitrogen liquefaction device to prepare high-purity oxygen Download PDFInfo
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- CN102252500A CN102252500A CN2011101214358A CN201110121435A CN102252500A CN 102252500 A CN102252500 A CN 102252500A CN 2011101214358 A CN2011101214358 A CN 2011101214358A CN 201110121435 A CN201110121435 A CN 201110121435A CN 102252500 A CN102252500 A CN 102252500A
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Abstract
The invention relates to a method for preparing high-purity oxygen and aims at provides a method which has the advantages of high yield, low investment, and lower cost. According to the technical scheme of the invention, the method for utilizing the oxygen-nitrogen liquefaction device to prepare high-purity oxygen comprises the following steps: a, a first rectifying tower evaporator, a first rectifying tower, a main condensate evaporator, a second rectifying tower, and a second rectifying tower condenser are sequentially and fixedly arranged from bottom to top, and then simultaneously carry out subsequent process; b, the nitrogen output by the oxygen-nitrogen liquefaction device absorbs cold energy so as to be converted into liquid nitrogen, the generated liquid nitrogen and the liquid nitrogen output by the oxygen-nitrogen liquefaction device are combined and release cold energy, and the cold energy is converted into a gaseous form so as to be returned the oxygen-nitrogen liquefaction device; and c, the liquid nitrogen output by the oxygen-nitrogen liquefaction device release cold energy, part of components are discharged, the other gas is divided into two paths: first-path gas absorbs cold energy, part of components of the first-path enter into the atmosphere for discharge, and the other components of the first-path is further rectified; and second-path gas absorbs cold energy part of components of the second-path gas enter into the atmosphere for discharge, and the other components of the second-path gas release cold energy, thus the products are obtained.
Description
Technical field
The present invention relates to a kind of air separating method, specifically is the method for producing high purity oxygen.
Background technology
Oxygen is prevalent in nature.People separate the highly purified oxygen of purifying out (〉=99.999%v/v adopt GB/T14599-2008 in term) by the kinds of processes method with it from compound or mixture, be widely used in the fields such as preparation, scientific research of production, photoelectricity industry, the normal mixture of integrated circuit and semiconductor devices now.The industrialized mass production high purity oxygen mainly realizes producing and purifying of oxygen by following three approach at present:
(1) water electrolysis+chemical method
(2) transformation absorption+chemical method
(3) cryogenic rectification method
Wherein: (one), (two) two kinds of its technical process of method are the process of gaseous oxygen, and its final product also is a gaseous state.By gas tank or metal pressing pressure container it is stored, realize the transportation of product, so amount is little and efficient is low.Simultaneously, the chemical method that adopts also forms certain restriction to commercial production scale.Not too be fit to remote transportation, not too be fit to a large amount of the storage.Also difficult adaptation modern enterprise is to the increasing demand of high purity oxygen.
(3) kind process is meant under low-temperature condition separates air.Its principle can be sketched and be: with raw air liquefaction, then according to the difference of the contained component of air (for example oxygen, nitrogen, argon) boiling point, adopt the method for cryogenic rectification to isolate oxygen, nitrogen, argon etc.The process route of this method general all extracts with argon, or krypton, xenon extract the high purity oxygen that combines and can directly obtain liquid state.Because argon, krypton, xenon etc. are rare gas, so it is all bigger to have the general scale of the air-separating plant of this class flow process, investment is also big certainly.In addition, be confined to air-separating plant and produce ability of cold (cold: industry slang refers generally to be lower than the energy value of atmospheric environment) and energy balance, the output of its high purity oxygen also is subjected to severely restricts.Just existing cryogenic rectification method can directly obtain liquid high purity oxygen, and it transports more convenient, efficient than (one) (two) two kinds of easier storages of method.But must rely on a large-scale space division device, amount of investment is very big, and output then is subjected to the quantitative limitation of air separation unit refrigeration.
Summary of the invention
Technical problem to be solved by this invention provides a kind of high purity oxygen preparation, and this method should have high purity oxygen product yield height, small investment, lower-cost characteristics.
Technical scheme provided by the invention is:
A kind of method of utilizing oxygen nitrogen liquefying plant to produce high purity oxygen, carry out according to the following steps:
A, with the first rectifying column evaporimeter, first rectifying column, main condenser evaporimeter, second rectifying column, second rectifying column condenser fixed and arranged successively from bottom to top, and the first rectifying column evaporimeter is connected with first rectifying column, and the main condenser evaporimeter is connected with second rectifying column; Carry out the subsequent job flow process then simultaneously;
The nitrogen of b, the output of oxygen nitrogen liquefying plant feeds the absorbing cavity of the first rectifying column evaporimeter, absorb and flow out first rectifying column after cold is converted to liquid nitrogen, merge with the liquid nitrogen of oxygen nitrogen liquefying plant output then and import the second rectifying column condenser again and emit cold, fail back oxygen nitrogen liquefying plant after being converted to gaseous form;
The liquid oxygen of c, the output of oxygen nitrogen liquefying plant is sent into first rectifying column and is emitted cold, wherein the evaporating temperature component that is higher than oxygen is discharged from the delivery pipe of the first rectifying column evaporimeter bottom, all the other heat absorption vaporized gas are divided into two-way: first via gas absorbs cold enter the absorbing cavity of main condenser evaporimeter by pipeline after, wherein the evaporating temperature component that is lower than oxygen enters airborne release with gaseous form, and all the other components are back to first rectifying column again with liquid form and continue rectification process; The second road gas absorbs cold by the absorbing cavity that pipeline enters the second rectifying column condenser, wherein the evaporating temperature component that is lower than oxygen enters airborne release with gaseous form, all the other components are back to second rectifying column with liquid form and emit cold, thereby obtain liquid high purity oxygen product;
Liquid oxygen evaporating temperature in the first rectifying column evaporimeter is less than the condensing temperature of nitrogen, and pressure and the control nitrogen gas pressure by the control liquid oxygen realizes respectively; Liquid nitrogen vaporization temperature in the second rectifying column condenser realizes by the pressure of control liquid nitrogen and the pressure of control oxygen respectively less than the condensing temperature of oxygen; Liquid oxygen evaporating temperature in the main condenser evaporimeter realizes by the pressure of control liquid oxygen and the pressure of oxygen respectively less than the condensing temperature of oxygen.
Among the described step C, the second road gas enters the second rectifying column condenser absorbing cavity in the following manner and absorbs cold: enter second rectifying column by a pipeline earlier, enter the second rectifying column condenser absorbing cavity by another pipeline more then with after gas in this rectifying column mixes.
Operation principle of the present invention is:
1, because the liquid oxygen pressure that liquefaction system is imported in first rectifying column is low, and liquefaction system is imported the nitrogen pressure height of the first rectifying column evaporimeter, so the condensing temperature that the evaporating temperature of liquid oxygen will be lower than nitrogen (for example: when the liquid oxygen pressure of first rectifying column among the embodiment is 0.188MPa, evaporating temperature is-176.8 ℃, and the nitrogen that liquefaction system provides is when pressure is 0.7MPa, condensing temperature is-174.6 ℃, 2.2 ℃ of both temperature difference).Like this, the evaporation of the condensation of nitrogen and liquid oxygen can be carried out simultaneously.
2, because the pressure of the interior rising oxygen of second rectifying column is low, and the liquid nitrogen pressure height that liquefaction system provides, so the condensing temperature that the evaporating temperature of liquid nitrogen will be lower than oxygen (for example: when the pressure of the rising oxygen in second rectifying column among the embodiment is 0.129MPa, condensing temperature is-180.8 ℃, and the liquid nitrogen that liquefaction system provides is when pressure is 0.4MPa, evaporating temperature is-181.9 ℃, 1.1 ℃ of both temperature difference).Like this, the evaporation of the condensation of oxygen and liquid nitrogen just can be carried out simultaneously.
3, because the pressure height of the interior rising oxygen of first rectifying column, and the liquid oxygen pressure that falls in second rectifying column is low, so the condensing temperature that the evaporating temperature of whereabouts liquid oxygen will be lower than rising oxygen (for example: when the rising oxygen pressure is 0.18MPa (A) in first rectifying column among the embodiment, condensing temperature is-177.5 ℃, and the second rectifying column whereabouts liquid oxygen pressure is 0.142MPa (A), evaporating temperature-179.8 ℃, 2.3 ℃ of both temperature difference).Like this, in the main condenser evaporimeter, the condensation of oxygen and the evaporation of liquid oxygen just can be carried out.
The invention has the beneficial effects as follows:
At first, the production procedure of rare gas such as the extraction argon that this method need not to rely on large-scale air separating technology device and it to attach troops to a unit, krypton, xenon, so a little order of magnitude is wanted in investment at least, flow process is more efficient, greatly reduces the production threshold of liquid high purity oxygen.Secondly, adopt this process only need do an increase configuration and can achieve the goal simple and easy to do instant effect existing oxygen nitrogen liquefying plant technological process.The 3rd, refrigerating capacity abundance, high purity oxygen output height.In addition, also have all advantages of cryogenic rectification method, and do not have the limitation of (two) two kinds of methods of background technology described ().
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is the structural representation of the first rectifying column evaporimeter among the present invention.
Fig. 3 is the second rectifying column structure of condenser schematic diagram among the present invention.
Fig. 4 is the structural representation of the main condenser evaporimeter among the present invention.
Fig. 5 is the structural representation of oxygen nitrogen liquefying plant.
The specific embodiment
The structure of existing oxygen nitrogen liquefying plant is as shown in Figure 5: the user for 2.0MPa nitrogen through decompressor impeller of booster BT supercharging, water cooler S is cooled to 40 ℃ of laggard main heat exchanger E1 of going into, enter refrigerator RU cooling from the extraction of main heat exchanger E1 middle part, advance main heat exchanger then and continue cooling; Afterwards, wherein a part extracts decompressor ET expansion out, provides liquefaction system needed most of cold, and the cryogen after the expansion enters main heat exchanger as cooling medium, goes out system after the re-heat; The liquefaction that in main heat exchanger E1, continues to be cooled of another part (fraction) nitrogen, going out to be throttled to behind the main heat exchanger E1 0.3MPa, to enter subcooler E2 cold excessively, the liquid nitrogen major part of crossing after cold enters the liquid nitrogen storage system as liquid nitrogen product (during the oxygen operating mode as backflowing low-temperature receiver), after a small amount of overfreezing liquid nitrogen throttling as the low-temperature receiver of subcooler, through subcooler E2, main heat exchanger E1, behind normal temperature, gone the circulatory system (low-pressure pipe network or nitrogen compressor inlet) successively by re-heat.
Middle pressure oxygen 1.6-2.5MPa from pipe network cools off and liquefaction deutomerite diffluence liquid oxygen storage system through oxygen heat exchanger E3.The low-temperature receiver of oxygen heat exchanger E3 is from nitrogen products, the nitrogen products major part in the oxygen heat exchanger re-heat to normal temperature; Fraction re-heat in the oxygen heat exchanger converges with the low pressure that the goes out subcooler E2 nitrogen that backflows after the uniform temperature, and re-heat is removed low-pressure pipe network or cyclic nitrogen press inlet to normal temperature in main heat exchanger E1.
The present invention is supporting utilize oxygen nitrogen liquefying plant after, have following characteristics:
1, has sufficient cold source
(3) plant cryogenic rectification method as previously mentioned, the output of high purity oxygen is subjected to a constraint; That is because the supporting refrigerating capacity of a whole set of air-separating plant is limited.In having the flow process of high purity oxygen, no matter extract argon, extract krypton, xenon all will consume abundant cold; Thereby the cold that the high purity oxygen part can be assigned to is very limited.The oxygen nitrogen liquefying plant of utilization of the present invention has very abundant refrigerating capacity, and the bottleneck of high purity oxygen on output is opened.
2, must adopt rectificating method to solve the purity problem of high purity oxygen
Because feed oxygen (the always industrial usually oxygen from oxygen nitrogen liquefying plant is directly adopted in the important pre-treatment of not extracting argon or extracting krypton, xenon part; Its impurity is formed more complicated), to methane wherein, other hydro carbons, and krypton, xenon component all must adopt rectificating method to purify; To adopt independent rectification process to remove methane especially to＜0.5 * 10
-6V/v.
Further specify by the following examples,
Embodiment:
A kind of method of utilizing oxygen nitrogen liquefying plant to produce high purity oxygen, carry out in the following manner:
A, with the first rectifying column evaporimeter K1, the first rectifying column C1, main condenser evaporimeter K, the second rectifying column C2, second rectifying column condenser K2 fixed and arranged successively from bottom to top, and the first rectifying column evaporimeter K1 is connected with the first rectifying column C1, and main condenser evaporimeter K is connected with the second rectifying column C2; Carry out the subsequent job flow process then simultaneously;
After feeding the absorbing cavity G1 of the first rectifying column evaporimeter K1, the nitrogen of b, oxygen nitrogen liquefying plant YD output absorbs cold, flow out first rectifying column after being converted to liquid nitrogen, then with the liquid nitrogen of oxygen nitrogen liquefying plant output merge import the second rectifying column condenser K2 again and emit cold after, become nitrogen and fail back oxygen nitrogen liquefying plant;
C, the liquid oxygen of oxygen nitrogen liquefying plant output is sent into first rectifying column and is emitted cold, wherein evaporating temperature is higher than the component (hydrocarbon of oxygen, krypton, xenon etc., mainly be methane) discharged (from the discharged of the first rectifying column evaporimeter K1 bottom to special-purpose storage tank), all the other heat absorption vaporized gas are divided into two-way: the first via absorbs cold by the absorbing cavity G that a pipeline enters main condenser evaporimeter K, wherein the evaporating temperature component (argon) that is lower than oxygen is discharged (entering atmosphere), and all the other components are back to first rectifying column with liquid form again by another pipeline and proceed rectifying; The second tunnel absorbing cavity G2 that enters the second rectifying column condenser absorbs cold, and (among the figure as can be known: this road gas enters second rectifying column by pipeline earlier, then with the absorbing cavity G2 that enters the second rectifying column condenser after other gas mixes again by another pipeline), wherein the evaporating temperature component that is lower than oxygen is discharged (entering atmosphere) by the floss hole of absorbing cavity G2, all the other components are back to second rectifier with liquid form and continue rectifying, obtain liquid high purity oxygen product from the output of second rectifying column then;
The liquid oxygen evaporating temperature of first rectifying column is less than the condensing temperature of nitrogen, and pressure and the control nitrogen gas pressure by the control liquid oxygen realizes respectively; The liquid nitrogen vaporization temperature of second rectifying column realizes by the pressure of control liquid nitrogen and the pressure of control oxygen respectively less than the condensing temperature of oxygen; The liquid oxygen evaporating temperature of main condenser evaporimeter realizes by the pressure of control liquid oxygen and the pressure of oxygen respectively less than the condensing temperature of oxygen.
The structure of described first rectifying column and second rectifying column is identical with the rectifying column structure of chemical industry equipment; The rectifying element can adopt filler+distributor internals, also can adopt sieve-plate structure, or the combined column structure of filler, sieve plate.
Absorbing cavity among evaporimeter K1, condenser K2 and the main condenser evaporimeter K can adopt plate-fin heat exchanger or pipe heat exchanger structure according to the needs of heat transfer temperature difference.
The present embodiment workflow is as follows:
Pipe network enters the liquefaction system heat exchanger for oxygen with pressure, utilizes the cold of liquefaction system will be with pressure oxygen liquefaction deutomerite to flow to into the participation rectifying of the above several theoretical plate positions of first rectifier bottoms; In first rectifying column, can remove component (hydrocarbon, krypton, the xenon etc. that evaporating temperature in the uprising gas is higher than oxygen by rectifying, mainly be to remove methane), liquid concentration among the evaporimeter K 1 hydrocarbon, total carbon content is higher, need discharge incessantly to guarantee safety.First rectifier obtains hydrocarbon-containiproducts gas seldom and enters the second rectifying column middle and upper part, wherein requires to remove methane to＜0.5 * 10
-7V/v is to guarantee that methane concentrates back purity still＜0.5 * 10 once more in the C2 tower
-6V/v.The effect of second rectifying column is the component (mainly being argon) that is lower than oxygen by evaporating temperature in the rectifying removal oxygen, has concentrated the argon component in the gaseous material of the second rectifying column condenser K2, needs incessantly to airborne release; In order to reduce discharge capacity, Extract oxygen product (by pipeline 13) is to the storage tank discharging from the second rectifying column condenser K2, and the liquid that several theoretical tray positions obtain more than second rectifier bottoms is argon content＜2 * 10
6The high purity oxygen product of v/v.From liquefaction system, get after the nitrogen throttling thermal source in the flow process as the first rectifying column evaporimeter K1, the liquid nitrogen throttling of coming out from evaporimeter K1 enters the second rectifying column condenser K2 as low-temperature receiver, the required cold energy insufficient section of the second rectifying column condenser K2 is replenished by the liquid nitrogen that liquefaction system provides, and the nitrogen throttling that the second rectifying column condenser K2 comes out is returned liquefaction system and reclaimed the residue cold energy.
The flow process characteristics:
1, this flow process material (hydrocarbon etc.) that at first the separating mixed gas mid-boiling point is high and then the low material (argon etc.) of separating mixed gas mid-boiling point.
2, from device, can obtain a large amount of liquid oxygen products, not produce low oxygen.
The recommending data of each pipeline in the present embodiment is as follows:
Equipment can be provided with cold insulated cabinet with liquefaction system in the present embodiment, also cold insulated cabinet can be set separately.
The structure of the first rectifying column evaporimeter K1 among the present invention as shown in Figure 2; The structure of the second rectifying column condenser K2 as shown in Figure 3; The structure of condenser/evaporator K as shown in Figure 4.These devices are outsourcing or self-control all.
Claims (3)
1. method of utilizing oxygen nitrogen liquefying plant to produce high purity oxygen, carry out according to the following steps:
A, with the first rectifying column evaporimeter (K1), first rectifying column (C1), main condenser evaporimeter (K), second rectifying column (C2), the second rectifying column condenser (K2) fixed and arranged successively from bottom to top, and the first rectifying column evaporimeter is connected with first rectifying column, and the main condenser evaporimeter is connected with second rectifying column; Carry out the subsequent job flow process then simultaneously;
The nitrogen of b, oxygen nitrogen liquefying plant (YD) output feeds the absorbing cavity (G1) of the first rectifying column evaporimeter, absorb and flow out first rectifying column after cold is converted to liquid nitrogen, merge with the liquid nitrogen of oxygen nitrogen liquefying plant output then and import the second rectifying column condenser (K2) again and emit cold, fail back oxygen nitrogen liquefying plant after being converted to gaseous form;
The liquid oxygen of c, the output of oxygen nitrogen liquefying plant is sent into first rectifying column and is emitted cold, wherein the evaporating temperature component that is higher than oxygen is discharged from the delivery pipe of first rectifying column evaporimeter (K1) bottom, all the other heat absorption vaporized gas are divided into two-way: first via gas absorbs cold by absorbing cavity (G) back that pipeline enters the main condenser evaporimeter, wherein the evaporating temperature component that is lower than oxygen enters airborne release with gaseous form, and all the other components are back to first rectifying column again with liquid form and continue rectification process; The second road gas absorbs cold by the absorbing cavity (G2) that pipeline enters the second rectifying column condenser, wherein the evaporating temperature component that is lower than oxygen enters airborne release with gaseous form, all the other components are back to second rectifying column (C2) with liquid form and emit cold, thereby obtain liquid high purity oxygen product.
2. a kind of method of utilizing oxygen nitrogen liquefying plant to produce high purity oxygen according to claim 1, it is characterized in that: the liquid oxygen evaporating temperature in the first rectifying column evaporimeter (K1) is less than the condensing temperature of nitrogen, and pressure and the control nitrogen gas pressure by the control liquid oxygen realizes respectively; Liquid nitrogen vaporization temperature in the second rectifying column condenser (K2) realizes by the pressure of control liquid nitrogen and the pressure of control oxygen respectively less than the condensing temperature of oxygen; Liquid oxygen evaporating temperature in the main condenser evaporimeter (K) realizes by the pressure of control liquid oxygen and the pressure of oxygen respectively less than the condensing temperature of oxygen.
3. a kind of method of utilizing oxygen nitrogen liquefying plant to produce high purity oxygen according to claim 1 and 2, it is characterized in that: among the described step C, the second road gas enters the second rectifying column condenser absorbing cavity (G2) in the following manner and absorbs cold: enter in second rectifying column by a pipeline earlier, then with the absorbing cavity that enters the second rectifying column condenser after gas in this rectifying column mixes again by another pipeline.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113063263A (en) * | 2021-04-29 | 2021-07-02 | 开封迪尔空分实业有限公司 | Air separation method for preparing liquid oxygen by using liquid nitrogen |
| CN113091401A (en) * | 2021-04-29 | 2021-07-09 | 开封迪尔空分实业有限公司 | Liquid air separation device for preparing liquid oxygen by using liquid nitrogen |
| CN116817541A (en) * | 2023-08-31 | 2023-09-29 | 齐齐哈尔黎明气体有限公司 | Medical oxygen filling process blowdown gas recovery device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113063263A (en) * | 2021-04-29 | 2021-07-02 | 开封迪尔空分实业有限公司 | Air separation method for preparing liquid oxygen by using liquid nitrogen |
| CN113091401A (en) * | 2021-04-29 | 2021-07-09 | 开封迪尔空分实业有限公司 | Liquid air separation device for preparing liquid oxygen by using liquid nitrogen |
| CN113091401B (en) * | 2021-04-29 | 2022-05-31 | 开封迪尔空分实业有限公司 | Liquid air separation device for preparing liquid oxygen by using liquid nitrogen |
| CN116817541A (en) * | 2023-08-31 | 2023-09-29 | 齐齐哈尔黎明气体有限公司 | Medical oxygen filling process blowdown gas recovery device |
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Application publication date: 20111123 |