CN102430337A - Low-temperature rectification system for producing stable isotope carbon-13 by using CO - Google Patents
Low-temperature rectification system for producing stable isotope carbon-13 by using CO Download PDFInfo
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- CN102430337A CN102430337A CN2011103553760A CN201110355376A CN102430337A CN 102430337 A CN102430337 A CN 102430337A CN 2011103553760 A CN2011103553760 A CN 2011103553760A CN 201110355376 A CN201110355376 A CN 201110355376A CN 102430337 A CN102430337 A CN 102430337A
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Abstract
The invention relates to a low-temperature rectification system for producing stable isotope carbon-13 by using CO; and the low-temperature rectification system is a cascade unit which comprises horizontally arranged n stages of rectifying towers, wherein each rectifying tower comprises an overhead condenser, a tower bottom reboiler and a rectifying column, and the rectifying towers at different stages are connected through the pipeline. Compared with the prior art, the low-temperature rectification system has the advantages that material conveying flow among the cascaded towers is reduced by arranging extracting sections in the horizontal cascaded towers and the cascade unit can be ensured to stably and continuously operate for long term.
Description
Technical field
The present invention relates to the stable isotope isolation technics of carbon, especially relate to a kind of employing cryogenic rectification CO production
13The low temperature distillation system of C.
Background technology
In the carbon compound, carbon is with stable isotope
12C,
13C and radioactivity
14C is present in occurring in nature, wherein
12C with
13The natural abundance ratio of C is about 98.9: 1.1.Along with development of science and technology,
13C has been widely used in fields such as medical science, pharmacology, biochemistry and life science as labelled atom.In addition, abundant
12The synthetic diamond of C also obtains paying close attention to than the better physical property of natural prodcuts.
In the prior art, multiple stable isotope has been arranged
13The production method of C, for example thermal diffusion method, gaseous diffusion process, chemical exchange method, cryogenic rectification method, laser method etc.Wherein cryogenic rectification method is to produce in the industry
13The main method of C, but because the vapour pressure between the isotope composition differs very little, obtain abundant carbon-13 and must adopt the multitower cascade operation.
As far back as 1949, Britain Harwell atomic energy research center just set up cryogenic rectification CO and has separated
13The device of C (T.F.Johns, H.London, enrichment of isotopes
13C and
18O, AERE Harwell reportG/R 661,1951), this device is made up of two towers connected vertically, and total length 32ft is in the product
13The C abundance is 60%, and productive rate is 0.4g
13C/d.
Former Soviet Union ladder Billy Si laboratory (П. Я. А с а mu а н u, B.A.
, Е. and Л.
, et al., П о л у ч e н и e и з о т о n а C
13м e т о л о м р e к т и ф и к а ц и и о к и с и у r л e р о л а, Isotopenpraxis, 4.Jahrgang; Heft 7,1968, and the CO hypothermia distillation device of 275-277) building is made up of three towers; This device total length 36m, first order tower diameter is 4.3cm, high 15m, second level tower diameter is 2.0cm, high 10m; Third level tower diameter is 1.0cm, high 11m, and three towers vertically connect.Filling triangle spiral coil filler in the tower, the insulation form is a vacuum insulation, in the product
13The C abundance is 60%.
In July, 1969, the U.S. builds up in Los Alamos laboratory cover CO hypothermia distillation device (D.E.Armstrong, an A.C.Briesmeister; B.B.Mclnteer, et a1., A carbon-13 production plant using carbon monoxide distillation; LASL report, LA-4391,1970); Be largest at that time CO hypothermia distillation device, this device is made up of seven sections towers that vertically are together in series, and puts into the vacuum jacket that diameter is 15.24cm together; Use polystyrene foam plastics and 40 layers of aluminium alloy Mylar film adiabatic again, put into 0.9144 meter of diameter, dark 38.1 meters paintpot at last.This device obtains through the balance period in 6 week
13The C abundance is 92.37% product.The 8kg/a's that this device back was built up in 1979
13The C device replaces (B.B.Mclnteer, isotope separation by distillation:design of a carbon-13 plant, separation science and technology; Vol.15, No.3,1980; 491-508); Be the Cola-Colita device, the king-tower of Cola-Colita device is made up of two sections towers that vertically are connected in series and isotopic transmutation reactions device and rectifying secondary tower, and wherein first section is 6 towers of long 100 meters; Second section 1 tower for 100 meters of length, long 55 meters of rectifying secondary tower.
1999, the Russian poplar. lattice. Chai Liewanxike (poplar. lattice. Chai Liewanxike, the vigorous. Ha Laoxilaofu of Ah., the cryogenic rectification oxycarbide prepares stable isotope, Х и м. and п р о м .1999, No.4 229-235) has designed a cover and has adopted the CO cryogenic rectification to separate
13The four tower cascade units of C, all the people present's tower adopts mode connected horizontally, and raw material joins the tower still of first order tower, and the 2nd～4 grade of tower all is enriching section, high design such as all the people present's tower employing, the height of inner-tower filling material is 20 meters.Gas material at the bottom of the prime Tata flows in the condenser of back level top of tower through the promotion of pressure automatically; Flow to back grade top of tower from the condenser bottom after the condensation; Spray liquid as back level tower; The steam of back level tower flows out from the top, and the process air blast is delivered to the bottom of prime tower, realizes the Flow of Goods and Materials between the cascade.This flow process has reduced the requirement to the place, but has increased the power conveying equipment of inter-stage material.
Comprehensive above document can be known, adopts the CO cryogenic rectification method to concentrate
13C need carry out the multitower cascade operation, and in the prior art, cascade unit has vertical cascade and two kinds of connected modes of horizontal cascade.In the vertical cascade, the liquid of prime tower relies on gravity to get into back level tower, and the steam of back level tower relies on pressure to get into the prime tower, realizes the mass transport between each tower of cascade easily.But because the number of theoretical plate of isotopic separation process need is a lot, cause tower very high, therefore, difficulty of construction is bigger; In addition,, reduce the separation of system because the pressure drop ratio of cascade unit is bigger, unfavorable to separating.Under comparing, the difficulty of construction of horizontal cascade is much little, still; In the horizontal cascade unit of the n of prior art level, the concentration that liquid and gas are kept in the charging of the 2nd～n level rectifying column cat head, discharging differs the difference of a α, so the mass flow between each tower of cascade is very big; Cause the energy consumption of conveying equipment bigger on the one hand; On the other hand, this cascade unit to the requirement of automatic control, instrument and meter than higher, and require every grade must be continuously, steady running; Accident appears in any one-level tower, all can cause the bad linking of cascade unit.
Summary of the invention
The object of the invention is exactly to provide a kind of cryogenic rectification CO to produce stable isotope for the defective that overcomes above-mentioned prior art existence
13The horizontal cascade system of C, this system can guarantee to have the separation than higher between isotope composition, and realize the operation that low temperature distillation system is long-term, stable easily.
The object of the invention can be realized through following technical scheme:
A kind of by CO production stable isotope
13The low temperature distillation system of C is the cascade unit that the n level rectifying column of horizontal positioned is formed, and wherein, said rectifying column is made up of overhead condenser, tower bottom reboiler and rectifying column, connects through pipeline between the rectifying columns at different levels.
The diameter of described n level rectifying column is tapered.
Described n level rectifying column is 2～10 grades of rectifying columns.
First order rectifying column can be from the middle part or cat head input raw material.
The steam of back level rectifying column cat head is transported to the tower middle part of prime rectifying column by gas transfer pump through pipeline in the described cascade unit, is transported to the middle part of back grade rectifying column after the liquid that the tower still of prime rectifying column produces vaporize in pipeline under pressure.
The steam of described back level rectifying column cat head can turn back to the feed points position of prime rectifying column.
The steam of described back level rectifying column cat head can turn back to the position higher than the feed points position of prime rectifying column.
The steam of described back level rectifying column cat head can turn back to the position lower than the feed points position of prime rectifying column.
Described gas transfer pump can be gas boosting pump, air blast, shielded electric pump, membrane pump or magnetic force driving pump.
Be filled with separating filler in the described rectifying column.
Described separating filler is metallic plate corrugated regular filler, woven wire structured packing, metal mesh opening ripple packing, grid packing or pulse filler.
Compared with prior art, the present invention is utilized in to be provided with in each tower of horizontal cascade and extracts section and reduce the mass transport flow between each tower of cascade, can guarantee long-term, stable, the running continuously of cascade unit.
Description of drawings
Fig. 1 is a cascade system sketch map of the present invention;
Fig. 2 is the schematic flow sheet of embodiment 1;
Fig. 3 is the concentration profile of each isotope composition in the embodiment 1 cascade rectifying column;
Fig. 4 is the schematic flow sheet of embodiment 2;
Fig. 5 is the concentration profile of each isotope composition in the embodiment 2 cascade rectifying columns.
The specific embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is elaborated.
Fig. 1 is the schematic flow sheet of the low temperature distillation system of being made up of n level rectifying column of the present invention, and this system is the cascade unit that is made up of n level rectifying column connected horizontally.In the cascade unit among the present invention, towers at different levels are to connect like this: raw material adds the middle part of the first order rectifying column of cascade unit, and the 1st grade of column overhead extraction part is low-abundance
13CO gas; A part of steam of the 1st～the n-1 level tower reboiler gasification gets into the middle part of the 2nd～the n level rectifying column after metering under pressure respectively; The part steam of the 2nd～the n level rectifying column cat head is delivered to the middle part of the 1st～the n-1 level rectifying column respectively through gas transfer pump; The steam part of the reboiler gasification of n level tower gets into the liquid that gets off with overhead condenser in the rectifying column and carries out gas, liquid mass transfer, and a part is abundant
13CO gas leaves cascade unit as product.
The cat head of the 1st grade～n level rectifying column connects condenser C1～Cn respectively; Each condenser all connects gas pipeline, the fluid pipeline that is communicated with rectifying column at the corresponding levels; With pipeline to previous stage rectifying column convey materials, in addition, each condenser also have cooling coagulate medium into and out of pipeline.
Overhead condenser C1～Cn can be coil exchanger, tubular heat exchanger, double pipe heat exchanger, plate type heat exchanger, spiral heat exchanger, plate-fin heat exchanger etc., preferred plate-fin heat exchanger.
In the cascade unit shown in Figure 1; The structured packing of filling high-specific surface area in the 1st～the n level rectifying Tata; Its type can be mellapak packing, grid packing, screen waviness structured packing, pulse filler etc., preferred perforated plate corrugated filler and screen waviness packings.
Connect reboiler B1～Bn respectively at the bottom of the tower of the 1st grade～n level rectifying column, each reboiler all connects the gas pipeline that is communicated with rectifying column at the corresponding levels, fluid pipeline and the pipeline of level rectifying column convey materials backward.
Back level column overhead material is delivered to the middle part of prime tower through gas transfer pump, and wherein said gas transfer pump can be gas boosting pump, air blast, shielded electric pump, membrane pump, magnetic force driving pump etc., preferred diaphragm pump.
With reference to Fig. 1; The CO raw material is delivered to the middle part of first order tower T1 by pipeline L3 via flowmeter F1 metering back; Filling separating filler in the T1 tower; For the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C1 and the tower bottom reboiler B1 provides the surface of heat transfer, mass transfer, take out abundant carbon-12 via pipeline L2 from the T1 cat head.Take out a part of steam from T1 tower still; Under the driving of pressure, measure the back is transported to tower T2 along pipeline L4 middle part via valve V1 and flowmeter F2; Filling separating filler in the T2 tower; For the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C2 and the tower bottom reboiler B2 provides the surface of heat transfer, mass transfer, take out a part of steam from the T2 cat head, be transported to the middle part of tower T1 along pipeline L5 by gas transfer pump P1.Take out a part of steam from T2 tower still; Under the driving of pressure, measure the back is transported to tower T3 along pipeline L6 middle part via valve V2 and flowmeter F3; Filling separating filler in the T3 tower; For the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C3 and the tower bottom reboiler B3 provides the surface of heat transfer, mass transfer, take out a part of steam from the T3 cat head, be transported to the middle part of tower T2 along pipeline L7 by gas transfer pump P2.Similarly, the 4th tower T4, the 5th tower T5 all adopt such connected mode up to n tower Tn.Tower still extraction abundant carbon-13 product at n tower Tn.
In the whole cascade unit; Column overhead pressure at different levels are identical, and the material that transmits between each tower of cascade is gas, and prime Tata still material is transported to the middle part of back level tower under pressure; Back level column overhead steam is transported to the middle part of previous stage tower by gas transfer pump; This cascade system can be guaranteed continuous, the stable operation of cascade unit, and because press operations such as each tower, the separation between isotope composition is also than higher.
In addition, also provide use above low temperature distillation system separation and concentration among the present invention
13During C, the Computer simulation results that the abundance of each isotope composition in the cascade unit distributes.Among the present invention, use the rectifying theory to carry out the design and the optimization of cascade unit, consider the influence of oxygen isotope in the system, investigate natural abundance in the computational process than higher
12C
16O,
13C
16O with
12C
18Three kinds of components of O.Cryogenic rectification cascade unit according to proposing among isotopic separation cascade theory and the present invention of precise distillation Design Theory also can obtain similar result.
Below in conjunction with embodiment the present invention is done further elaboration.
Cascade unit among the embodiment 1 is made up of 4 grades of rectifying columns, and the process flow diagram of cascade unit is as shown in Figure 2.The CO raw material is delivered to the middle part of first order tower T1 by pipeline L3 through flowmeter F1 metering back, the interior filling metal screen waviness packings of T1 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C1 and the tower bottom reboiler B1.Take out abundant carbon-12 from the T1 cat head via pipeline L2, take out a part of steam, under the driving of pressure, measure the back is transported to tower T2 along pipeline L4 middle part via valve V1 and flowmeter F2 from T1 tower still.Filling metal screen waviness packings in the T2 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C2 and the tower bottom reboiler B2.Take out a part of steam from the T2 cat head; Be transported to the middle part of tower T1 along pipeline L5 by membrane pump P1; Raw material with natural abundance joins among the tower T1, takes out a part of steam from T2 tower still, under the driving of pressure, measures the back is transported to tower T3 along pipeline L6 middle part via valve V2 and flowmeter F3.Filling metal screen waviness packings in the T3 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C3 and the tower bottom reboiler B3.Take out a part of steam from the T3 cat head; Be transported to the middle part of tower T2 along pipeline L7 by membrane pump P2; Wherein pipeline L7 is connected with tower T2 at same position with pipeline L4; Take out a part of steam from T3 tower still, under the driving of pressure, measure the back is transported to tower T4 along pipeline L8 middle part via valve V3 and flowmeter F4.Filling metal screen waviness packings in the T4 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C4 and the tower bottom reboiler B4.Take out a part of steam from the T4 cat head, be transported to the middle part of tower T3 by membrane pump P3 along pipeline L9, wherein pipeline L6 is connected with tower T3 at same position with pipeline L9, at the tower still B4 of the 4th tower T4 extraction abundant carbon-13 product.
Among the embodiment 1, raw material is that carbon-13 abundance is 1.1% natural CO, after the separation through the level Four tower, and carbon-13 enrichment to 90%, table 1 is to produce per year only
13C 100kg, abundance are the technological parameter of 90% cascade unit, and the isotope abundance in each tower of cascade distributes as shown in Figure 3.
The level Four of producing 100kg carbon-13 among table 1 embodiment 1 per year joins technological parameters of device
Data from table 1 can be found out; The inventory that the inventory that level tower in back turns back to the prime tower is vaporized in the reboiler at the bottom of the level Tata of back; Reduced the stagnant material amount in the connecting line between each tower of cascade, and middle cascade tower can carry out single tower total reflux operation when going wrong; Cascade unit is linked up after the problem of treating solves, cascade unit can very fast recovery operation again.Because column overhead pressure at different levels are identical, have between isotope composition than higher separation.
Cascade unit among the embodiment 2 is made up of 4 grades of rectifying columns, and the process flow diagram of cascade unit is as shown in Figure 4.The CO raw material is delivered to the middle part of first order tower T1 by pipeline L3 via flowmeter F1 metering back; Filling metal screen waviness packings in the T1 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C1 and the tower bottom reboiler B1.Take out abundant carbon-12 from the T1 cat head via pipeline L2, take out a part of steam, under the driving of pressure, measure the back is transported to tower T2 along pipeline L4 middle part (Fig. 4 mid point d position) via valve V1 and flowmeter F2 from T1 tower still.Filling metal screen waviness packings in the T2 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C2 and the tower bottom reboiler B2.Take out a part of steam from the T2 cat head, be transported to the position (Fig. 4 mid point a position) on the lower side, middle part of tower T1 by membrane pump P1 along pipeline L5.Take out a part of steam from T2 tower still, under the driving of pressure, measure the back is transported to tower T3 along pipeline L6 middle part (Fig. 4 mid point h position) via valve V2 and flowmeter F3.Filling metal screen waviness packings in the T3 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C3 and the tower bottom reboiler B3.Take out a part of steam from the T3 cat head; Be transported to the position (Fig. 4 mid point e position) on the lower side, middle part of tower T2 along pipeline L7 by membrane pump P2; Take out a part of steam from T3 tower still, under the driving of pressure, measure the back is transported to tower T4 along pipeline L8 middle part (Fig. 4 mid point 1 position) via valve V3 and flowmeter F4.Filling metal screen waviness packings in the T4 tower provides the surface of heat transfer, mass transfer for the steam of vaporizing among the liquid of condensing reflux among the overhead condenser C4 and the tower bottom reboiler B4.Take out a part of steam from the T4 cat head, be transported to the position (Fig. 4 mid point i position) on the lower side, middle part of tower T3 by membrane pump P3 along pipeline L9, at tower still extraction abundant carbon-13 product of the 4th tower T4.
Among the embodiment 2; Raw material is that carbon-13 abundance is 1.1% natural CO, after the separation through the level Four tower, and carbon-13 enrichment to 90%; Table 1 is to produce the technological parameter that 100kg, abundance are the cascade unit of 90% clean carbon-13 per year, and the isotope abundance in each tower of cascade distributes as shown in Figure 5.
The level Four of producing 100kg carbon-13 among table 2 embodiment 1 per year joins technological parameters of device
Data from table 2 can be found out; The inventory that the inventory that level tower in back turns back to the prime tower is vaporized in the reboiler at the bottom of the level Tata of back; Reduced the stagnant material amount in the connecting line between each tower of cascade, and middle cascade tower can carry out single tower total reflux operation when going wrong; Cascade unit is linked up after the problem of treating solves, cascade unit can very fast recovery operation again.Because column overhead pressure at different levels are identical, have between isotope composition than higher separation.
Embodiment 3
A kind of by CO production stable isotope
13The low temperature distillation system of C is 2 grades of diameters of horizontal positioned cascade unit that rectifying column forms that is tapered, and wherein, rectifying column is made up of overhead condenser, tower bottom reboiler and rectifying column, connects through pipeline between the rectifying columns at different levels.First order rectifying column can be imported raw material from the middle part.The steam of back level rectifying column cat head is transported to the tower middle part of prime rectifying column by gas transfer pump through pipeline in the cascade unit, is transported to the middle part of back grade rectifying column after the liquid that the tower still of prime rectifying column produces vaporize in pipeline under pressure.The steam of back level rectifying column cat head can turn back to the feed points position of prime rectifying column.The gas transfer pump of using is the gas boosting pump, in rectifying column, is filled with grid packing as separating filler.
Embodiment 4
A kind of by CO production stable isotope
13The low temperature distillation system of C is 10 grades of diameters of horizontal positioned cascade unit that rectifying column forms that is tapered, and wherein, rectifying column is made up of overhead condenser, tower bottom reboiler and rectifying column, connects through pipeline between the rectifying columns at different levels.First order rectifying column can be imported raw material from cat head.The steam of back level rectifying column cat head is transported to the tower middle part of prime rectifying column by gas transfer pump through pipeline in the cascade unit, is transported to the middle part of back grade rectifying column after the liquid that the tower still of prime rectifying column produces vaporize in pipeline under pressure.The steam of back level rectifying column cat head can turn back to the feed points position of prime rectifying column, also can turn back to the position higher than the feed points position of prime rectifying column, can also turn back to the position lower than the feed points position of prime rectifying column.The gas transfer pump of using is air blast or magnetic force driving pump.Be filled with in the rectifying column and belong to silk screen structured packing, metal mesh opening ripple packing as separating filler.
Although the embodiment in conjunction with concrete has been described native system, those skilled in the art can recognize in this area has various other embodiment in the scope of claim of the present invention and spirit.
Claims (11)
1. produce stable isotope by CO for one kind
13The low temperature distillation system of C is characterized in that, this system is the cascade unit that the n level rectifying column of horizontal positioned is formed, and wherein, said rectifying column is made up of overhead condenser, tower bottom reboiler and rectifying column, connects through pipeline between the rectifying columns at different levels.
2. according to claim 1 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, the diameter of described n level rectifying column is tapered.
3. according to claim 1 and 2 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, described n level rectifying column is 2～10 grades of rectifying columns.
4. according to claim 1 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, first order rectifying column can be from the middle part or cat head input raw material.
5. according to claim 1 a kind of by CO production stable isotope
13The low temperature distillation system of C; It is characterized in that; The steam of back level rectifying column cat head is transported to the tower middle part of prime rectifying column by gas transfer pump through pipeline in the described cascade unit, is transported to the middle part of back grade rectifying column after the liquid that the tower still of prime rectifying column produces vaporize in pipeline under pressure.
6. according to claim 5 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, the steam of described back level rectifying column cat head can turn back to the feed points position of prime rectifying column.
7. according to claim 5 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, the steam of described back level rectifying column cat head can turn back to the position higher than the feed points position of prime rectifying column.
8. according to claim 5 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, the steam of described back level rectifying column cat head can turn back to the position lower than the feed points position of prime rectifying column.
9. according to claim 5 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, described gas transfer pump can be gas boosting pump, air blast, shielded electric pump, membrane pump or magnetic force driving pump.
10. according to claim 1 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, is filled with separating filler in the described rectifying column.
11. it is according to claim 10 a kind of by CO production stable isotope
13The low temperature distillation system of C is characterized in that, described separating filler is metallic plate corrugated regular filler, woven wire structured packing, metal mesh opening ripple packing, grid packing or pulse filler.
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| CN113813786A (en) * | 2020-06-19 | 2021-12-21 | 核工业理化工程研究院 | Quasi-rectangular cascade separation method, rectangular cascade improvement method and application thereof |
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| CN108592520A (en) * | 2018-04-13 | 2018-09-28 | 杭州杭氧股份有限公司 | A kind of technical grade produces the method and device of 18O isotopes using cryogenic rectification |
| CN108592520B (en) * | 2018-04-13 | 2020-10-27 | 杭州制氧机集团股份有限公司 | Method and device for producing 18O isotope by industrial-grade cryogenic rectification |
| CN110420561A (en) * | 2019-07-24 | 2019-11-08 | 邯郸钢铁集团有限责任公司 | Neon isotope separator and separation method |
| CN113813786A (en) * | 2020-06-19 | 2021-12-21 | 核工业理化工程研究院 | Quasi-rectangular cascade separation method, rectangular cascade improvement method and application thereof |
| CN112156653A (en) * | 2020-10-10 | 2021-01-01 | 湖北楚儒同位素科技有限公司 | Low-temperature separation and concentration device and process for stable isotopes |
| CN112156653B (en) * | 2020-10-10 | 2023-08-22 | 湖北楚儒同位素科技有限公司 | Stable isotope low-temperature separation and concentration device and process |
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