CN102773016A - Method and device for separately producing enriched boron-10 (10B) by using multiple serial towers - Google Patents
Method and device for separately producing enriched boron-10 (10B) by using multiple serial towers Download PDFInfo
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- CN102773016A CN102773016A CN2012102340102A CN201210234010A CN102773016A CN 102773016 A CN102773016 A CN 102773016A CN 2012102340102 A CN2012102340102 A CN 2012102340102A CN 201210234010 A CN201210234010 A CN 201210234010A CN 102773016 A CN102773016 A CN 102773016A
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Abstract
The invention relates to a method and device for separately producing enriched boron-10 (10B) by using multiple serial towers. In the method, enriched production of 10B is realized through multiple chemical exchange towers which are connected in series. The production device mainly comprises a complexing tower, serial chemical exchange towers, and a cracking tower, wherein the tower top of the cracking tower is provided with a condenser; the tower bottom of the cracking tower is provided with a heating kettle; and continuous flow of a liquid phase is realized among the complexing tower, each chemical exchange tower and the cracking tower through a pump. A liquid phase sprayed out of the complexing tower is pumped to the top of the first chemical exchange tower through a pump, and is pumped to the top of the second chemical exchange tower after flowing out of the bottom of the first chemical exchange tower till the liquid phase flowing out of the bottom of the last exchange tower is pumped to the top of the cracking tower; and a liquid phase flowing out of the bottom of the cracking tower is subjected to heat exchange through a heat exchanger, and is pumped to the top of the complexing tower through a pump, so that circular flow of the liquid phase among serial towers is formed. Due to the adoption of the method and the device, production of enriched 10B is realized through multiple serial towers, the abundance of the boron-10 is over 95 percent, and the abundance requirement of an enriched 10B product in the fields of nuclear power, military industry, aerospace and the like is met.
Description
Technical field
The present invention relates to separation technology field, particularly isotopic separation technology is applicable to fields such as national defence, military project, Aero-Space, nuclear industry, provide different abundance (abundance refers to a certain type of shared ratio of atom in the isotope) needs enrichment boron-10 (
10B) production technology.
Background technology
Stable isotope boron-10 (
10B) application of aspects such as nuclear industry, military equipment and medicine is increasingly extensive in modern times because of it has unique absorption characteristic to neutron.Enrichment
10The B product comprises boron-10 acid that different abundance require, boron-10 powder, and boron carbide, series of products such as boron nitride, the industry chain length, product applications is extensive, particularly plays an important role to alleviating the nervous problem of global fossil energy.This series products is applied to the nuclear energy field, and the nuclear energy resource that makes extensive exploitation use economy, safety, cleaning becomes possibility.
The Chemical Exchange rectification method of boron trifluoride methyl phenyl ethers anisole is the technology of U.S.'s initiative, in middle nineteen seventies starting in last century, reaches product in 1977,2 tons/year production scale, and 10 boron abundance are 92%.This technology, because of under normal temperature, condition of normal pressure, operating, and higher separation and show advantage.The flow process of first, etherate material is slightly long though feedstock production methyl phenyl ethers anisole complex compound is compared, and its basic material methyl phenyl ethers anisole is recycling in the whole process in production system, and final products be after the enrichment boron trifluoride-10 (
10BF
3) and boron trifluoride-11 (
11BF
3), these two kinds of article are the high terminal technology product of added value, aspect the cost and benefit accounting, have clear superiority than first, ether method, make production cost low.The U.S. and Georgia all adopt this processing technology routine at present.
But because this technological process is long, branch's operation is more, operation is complicated, the suitability for industrialized production difficulty is bigger.Especially to reach high abundance
10The B separation requirement, required Chemical Exchange tower number of theoretical plate is many, and tower height surpasses hundred meters, for reducing the device height requirement, reduces the realization of industrialization difficulty, and the present invention adopts the form of multitower series connection to realize high abundance
10Process of industrialization has been accelerated in the enrichment production of B.
Summary of the invention
The present invention will adopt the Chemical Exchange rectification method to produce boron istope.In process of production, adopt boron trifluoride-methyl phenyl ethers anisole Chemical Exchange rectification process route, the BF of rising
3The liquid phase C of gas and decline
6H
5OCH
3BF
3Carry out mass transfer and exchange through high efficiency packing, last
10B at the bottom of tower at leisure enrichment get up, reach the purpose of separation.
Multitower series connection separation of produced enrichment boron-10 of the present invention (
10B) the method and the technical scheme of device are following:
A kind of device of multitower series connection separation of produced enrichment boron-10 is characterized in that realizing with the mode of Chemical Exchange tower multitower series connection
10The enrichment production of B; Process units mainly comprises Chemical Exchange tower (3), the cleavage column (4) of complexing tower (2), series connection; The cleavage column cat head is provided with heating kettle at the bottom of being provided with condenser (5), tower; Pass through the continuous-flow that pump is realized liquid phase between complexing tower, each Chemical Exchange tower and the cleavage column.
In the complexing tower spray and under liquid phase beat to first Chemical Exchange cat head by pump; After going out from tower bottom flow again through pump to the second a Chemical Exchange cat head; Liquid phase until at the bottom of last root exchange column, coming out is beaten to the cleavage column top by pump; The liquid phase that bottom cleavage column, flows out is beaten to the complexing cat head by pump through after heat exchanger (6) heat exchange, thereby forms liquid phase circulating between column in series.
Multitower series connection separation of produced enrichment boron-10 of the present invention (
10B) method adopts methyl phenyl ethers anisole Chemical Exchange rectification method; The BF3 unstripped gas gets into from the complexing tower bottom, and methyl phenyl ethers anisole is down instead given birth to complex reaction and produced boron trifluoride-methyl phenyl ethers anisole liquid complexing thing under 10-25 ℃ of condition with the cat head spray, by the outflow of complexing tower bottom, squeezes into exchange column through pump; Cracking reaction takes place in the boron trifluoride-methyl phenyl ethers anisole liquid complexing thing that pumps in the cleavage column through exchange column under 140-170 ℃ of conditions, the BF that cracking produces
3Gas is got into by the exchange column bottom behind overhead condensation, keeps exchange column under 20-30 ℃ of operating conditions, BF
3Chemical exchange reaction takes place in gas and boron trifluoride-methyl phenyl ethers anisole liquid complexing thing counter current contacting,
10Progressively enrichment in liquid phase of B moves in circles successively, until
10The B abundance reaches more than 95%.
The extraction mode can be passed through
10BF
3Outlet with
10BF
3The extraction of gas products form, or export with boron trifluoride-methyl phenyl ethers anisole liquid complexing produce article form extraction through boron trifluoride-methyl phenyl ethers anisole liquid complexing thing.The form of extraction product can be confirmed according to the needs of subsequent product.
11BF
3Gas vent is the enrichment of by-product
11BF
3Gas extraction mouth.
The Chemical Exchange tower can be many series connection, confirms the height and the number of tower as required with factory building.
In the complexing tower, but methyl phenyl ethers anisole complexing agent fast Absorption boron trifluoride forms the boron trifluoride methyl phenyl ethers anisole compound of 1:1.The complex reaction that boron trifluoride and methyl phenyl ethers anisole complexing agent carry out is the heat release reversible reaction, reduces temperature to 10-25 ℃, and the reaction nature carries out to the complexing direction.When complex compound is heated to 140-170 ℃, will cracking become boron trifluoride and methyl phenyl ethers anisole complexing agent.So, boron trifluoride methyl phenyl ethers anisole complex compound fully contacts in the Chemical Exchange tower with boron trifluoride, has realized the boron istope chemical exchange reaction between the gas-liquid phase, and reactional equation is following:
Because
10BF
3With
11BF
3Volatility different, under the Chemical Exchange effect of 15-30 ℃ of temperature,
10B is enriched in the liquid phase, and
11B is enriched in the gas phase.The complex compound of liquid phase through end backflow effect, gets into cleavage column after carrying out Chemical Exchange, complex compound is heated there, and cracking becomes boron trifluoride-10 and corresponding complexing agent.Gas phase rises to exchange column through condenser pipe, enters into the complexing tower then.Complexing agent after the cracking and boron trifluoride complexing again become complex compound.Form the circulatory system of a closure like this.Need replenish chemical substance hardly in the reflux course, have only the consumption of energy.
Because the separation of boron istope needs hundreds of piece number of theoretical plate, the abundance of target product requires high more, and required number of theoretical plate is also high more.If in a Chemical Exchange tower, realize enrichment, often need tens meters even up to a hundred meters high, the realization of industrialization difficulty is bigger.For this reason, adopt multitower series connection form to carry out Chemical Exchange, reduce equipment requirements, accelerate process of industrialization.Through The effects and operation operation, the Chemical Exchange system of multitower series connection satisfies the concentration and separation of boron istope fully,
10The B product can reach more than 95%.
Whole technical process has formed the multitower series connection, mainly comprises a complexing tower, many exchange columns and a cleavage column.Each tower bottom is respectively established a tower still and a flow pump, and each tower still is provided with the liquid sampling mouth, can control the enrichment that different abundance are required
10The extraction of B product.
Patent art adopts the multitower series connection to realize enrichment
10The production of B, boron-10 abundance reaches more than 95%, satisfies multi-field enrichments such as nuclear power, military project, Aero-Space
10The requirement of B product abundance.
Description of drawings
Fig. 1: multitower series connection separation of produced enrichment
10The process chart of B;
1.BF
3The unstripped gas steel cylinder; 2. complexing tower; 3. Chemical Exchange tower; 4. cleavage column; 5. heating kettle; 6. heat exchanger; 7.
11BF
3Gas; 8.
10BF
3Product gas; 9.
10BF
3Methyl phenyl ethers anisole liquid complexing thing.
The specific embodiment
Raw material 1: the boron triflouride gas of natural abundance and methyl phenyl ethers anisole.
Install as shown in the figure: the mode with the series connection of Chemical Exchange tower multitower, realize
10The enrichment production of B; Process units mainly comprises Chemical Exchange tower (3), the cleavage column (4) of complexing tower (2), series connection; The cleavage column cat head is provided with heating kettle (5) at the bottom of being provided with condenser, tower; Pass through the continuous-flow that pump is realized liquid phase between complexing tower, each Chemical Exchange tower and the cleavage column.
In the complexing tower spray and under liquid phase beat to first Chemical Exchange cat head by pump; After going out from tower bottom flow again through pump to the second a Chemical Exchange cat head; Liquid phase until at the bottom of last root exchange column, coming out is beaten to the cleavage column top by pump; The liquid phase that bottom cleavage column, flows out is beaten to the complexing cat head by pump through after heat exchanger (6) heat exchange, thereby forms liquid phase circulating between column in series.
This technology is mainly passed through BF
3The BF of gas and liquid phase
3The methyl phenyl ethers anisole complex compound carries out chemical exchange reaction,
10B enrichment at the bottom of exchange column gradually can obtain three series products of different abundance in the whole system:
11BF
3Gas (7),
10BF
3Gas (8) and
10BF
3Methyl phenyl ethers anisole liquid complexing thing (9) all can be used as the raw materials for production of downstream enrichment boron product.Through adopting the multitower series system also to make enrichment boron-10 product that basic, normal, high different abundance are required in a covering device, can obtain simultaneously, the tower still at the bottom of each exchange column is provided with the product sample tap, and product form is enrichment
10BF
3Methyl phenyl ethers anisole liquid complexing thing.
Instance one: boron trifluoride unstripped gas (1) gets into the complexing tower from the bottom, forms the boron trifluoride methyl phenyl ethers anisole compound of 1:1 with the excessive methyl phenyl ethers anisole under the overhead streams.The complex reaction that boron trifluoride and methyl phenyl ethers anisole complexing agent carry out is the heat release reversible reaction, reduces temperature to 10-15 ℃, and the reaction nature carries out to the complexing direction.When complex compound is heated to 140-150 ℃, will cracking become boron trifluoride and methyl phenyl ethers anisole complexing agent.In 15-20 ℃ Chemical Exchange system; The boron triflouride gas that cracking is come rises from the exchange column bottom, with the boron trifluoride-methyl phenyl ethers anisole complex compound counter current contacting that descends from cat head, exchange reaction takes place; Move in circles the last enrichment that at the bottom of exchange column, obtains 95% above abundance
10The B product.
Instance two: the boron trifluoride unstripped gas gets into the complexing tower from the bottom, forms the boron trifluoride methyl phenyl ethers anisole compound of 1:1 with the excessive methyl phenyl ethers anisole under the overhead streams.The complex reaction that boron trifluoride and methyl phenyl ethers anisole complexing agent carry out is the heat release reversible reaction, reduces temperature to 15-20 ℃, and the reaction nature carries out to the complexing direction.When complex compound is heated to 150-160 ℃, will cracking become boron trifluoride and methyl phenyl ethers anisole complexing agent.In 20-25 ℃ Chemical Exchange system; The boron triflouride gas that cracking is come rises from the exchange column bottom, with the boron trifluoride-methyl phenyl ethers anisole complex compound counter current contacting that descends from cat head, exchange reaction takes place; Move in circles the last enrichment that at the bottom of exchange column, obtains 95% above abundance
10The B product.
Instance three: the boron trifluoride unstripped gas gets into the complexing tower from the bottom, forms the boron trifluoride methyl phenyl ethers anisole compound of 1:1 with the excessive methyl phenyl ethers anisole under the overhead streams.The complex reaction that boron trifluoride and methyl phenyl ethers anisole complexing agent carry out is the heat release reversible reaction, reduces temperature to 20-25 ℃, and the reaction nature carries out to the complexing direction.When complex compound is heated to 160-170 ℃, will cracking become boron trifluoride and methyl phenyl ethers anisole complexing agent.In 25-30 ℃ Chemical Exchange system; The boron triflouride gas that cracking is come rises from the exchange column bottom, with the boron trifluoride-methyl phenyl ethers anisole complex compound counter current contacting that descends from cat head, exchange reaction takes place; Move in circles the last enrichment that at the bottom of exchange column, obtains 95% above abundance
10The B product.
Enrichment of the present invention
10The production technology of B, those skilled in the art can be through using for reference this paper content, and links such as appropriate change technological parameter, structural design realize.System of the present invention is described through various embodiment, and person skilled obviously can be changed or suitably change and combination system as herein described in not breaking away from content of the present invention, spirit and scope, realizes the present invention's technology.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as and are included in spirit of the present invention, scope and the content.
Claims (3)
1. the device of a multitower series connection separation of produced enrichment boron-10 is characterized in that realizing with the mode of Chemical Exchange tower multitower series connection
10The enrichment production of B; Process units mainly comprises Chemical Exchange tower 3, the cleavage column 4 of complexing tower 2, series connection; The cleavage column cat head is provided with heating kettle at the bottom of being provided with condenser, tower; Pass through the continuous-flow that pump is realized liquid phase between complexing tower, each Chemical Exchange tower and the cleavage column.
2. device as claimed in claim 1; It is characterized in that in the complexing tower spray and under liquid phase beat to first Chemical Exchange cat head by pump; Again through pump to the second a Chemical Exchange cat head, beaten to the cleavage column top by pump until the liquid phase of at the bottom of last root exchange column, coming out after going out from tower bottom flow, the liquid phase that is flowed out by the cleavage column bottom is through after heat exchanger 6 heat exchange; Beat to the complexing cat head by pump, thereby form liquid phase circulating between column in series.
3. the method for the multitower of claim 1 series connection separation of produced enrichment boron-10 is characterized in that adopting methyl phenyl ethers anisole Chemical Exchange rectification method; BF
3Unstripped gas gets into from the complexing tower bottom, and methyl phenyl ethers anisole is down instead given birth to complex reaction and produced boron trifluoride-methyl phenyl ethers anisole liquid complexing thing under 10-25 ℃ of condition with the cat head spray, by the outflow of complexing tower bottom, squeezes into exchange column through pump; Cracking reaction takes place in the boron trifluoride-methyl phenyl ethers anisole liquid complexing thing that pumps in the cleavage column through exchange column under 140-170 ℃ of conditions, the BF that cracking produces
3Gas gets into from the exchange column bottom behind overhead condensation, keeps exchange column under 20-30 ℃ of operating conditions, BF
3Chemical exchange reaction takes place in gas and boron trifluoride-methyl phenyl ethers anisole liquid complexing thing counter current contacting,
10Progressively enrichment in liquid phase of B moves in circles successively, until
10The B abundance reaches more than 95%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102340102A CN102773016A (en) | 2012-07-06 | 2012-07-06 | Method and device for separately producing enriched boron-10 (10B) by using multiple serial towers |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102340102A CN102773016A (en) | 2012-07-06 | 2012-07-06 | Method and device for separately producing enriched boron-10 (10B) by using multiple serial towers |
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| CN2012102340102A Pending CN102773016A (en) | 2012-07-06 | 2012-07-06 | Method and device for separately producing enriched boron-10 (10B) by using multiple serial towers |
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Cited By (14)
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|---|---|---|---|---|
| CN104190256A (en) * | 2014-08-16 | 2014-12-10 | 刘小秦 | Construction method based on technology for producing boron isotope by anisole-boron trifluoride |
| CN104209003A (en) * | 2014-08-16 | 2014-12-17 | 刘小秦 | Industrial production method for separating boron isotope product based on methyl-phenoxide-boron trifluoride complex |
| CN104230972A (en) * | 2014-08-16 | 2014-12-24 | 刘小秦 | Method for purifying anisole-boron trifluoride complex |
| CN104944432A (en) * | 2015-06-30 | 2015-09-30 | 莱芜亚赛陶瓷技术有限公司 | Superfine 10B-rich titanium diboride powder and preparation method thereof |
| CN105664718A (en) * | 2016-01-22 | 2016-06-15 | 渤海大学 | Method for isolating and producing enriched 28Si, 29Si and 30Si by serially connected multiple towers and apparatus used by method |
| CN108275691A (en) * | 2018-04-13 | 2018-07-13 | 壹号元素（广州）科技有限公司 | Method and system that are a kind of while producing -11 boron trifluoride of -10 boron trifluoride of highly concentrated boron and highly concentrated boron |
| CN110735208A (en) * | 2019-09-03 | 2020-01-31 | 刘禹超 | Industrial production method of neutron radiation protection fiber materials |
| CN111282438A (en) * | 2020-04-01 | 2020-06-16 | 辽宁鸿昊化学工业股份有限公司 | High abundance10B isotope enrichment method |
| CN111389224A (en) * | 2020-03-30 | 2020-07-10 | 辽宁鸿昊化学工业股份有限公司 | Method for enriching boron-10 isotope anti-blocking tower by distillation method |
| RU2729797C1 (en) * | 2019-12-27 | 2020-08-12 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Российский химико-технологический университет имени Д.И. Менделеева" (РХТУ им. Д.И. Менделеева) | Mass transfer column |
| CN113750797A (en) * | 2021-09-15 | 2021-12-07 | 黑龙江豪运药业有限公司 | Device and method for separating high-abundance isotope boron 11 boron trifluoride by low-temperature vacuum rectification boron trifluoride |
| CN115608156A (en) * | 2022-12-19 | 2023-01-17 | 淄博颐康环保科技有限公司 | Sectional type cooling complexing device and complexing method for separating boron isotopes |
| CN116688756A (en) * | 2023-08-03 | 2023-09-05 | 天津天和盛新材料科技有限公司 | Continuous production process method for separating boron isotopes |
| CN116832615A (en) * | 2023-08-29 | 2023-10-03 | 天津天和盛新材料科技有限公司 | Continuous production process method for silicon isotopes |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1864821A (en) * | 2006-04-18 | 2006-11-22 | 天津大学 | Three tower cascade connected, single tower accumulating, total refluxing and batch collecting alternative operating method for boron-10 separation |
| CN202778278U (en) * | 2012-07-06 | 2013-03-13 | 天津大学 | Device for separating and producing enriched boron-10 (<10>B) by multiple serial towers |
-
2012
- 2012-07-06 CN CN2012102340102A patent/CN102773016A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1864821A (en) * | 2006-04-18 | 2006-11-22 | 天津大学 | Three tower cascade connected, single tower accumulating, total refluxing and batch collecting alternative operating method for boron-10 separation |
| CN202778278U (en) * | 2012-07-06 | 2013-03-13 | 天津大学 | Device for separating and producing enriched boron-10 (<10>B) by multiple serial towers |
Non-Patent Citations (3)
| Title |
|---|
| YIPING HUANG等: "Research on chemical exchange process of boron isotope separation", 《PROCEDIA ENGINEERING》 * |
| 叶定岳等: "关于同位素硼-10 的分离和生产", 《精细化工》 * |
| 谭国锋: "硼同位素分离的研究", 《工程科技Ⅰ辑》 * |
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| CN104190256A (en) * | 2014-08-16 | 2014-12-10 | 刘小秦 | Construction method based on technology for producing boron isotope by anisole-boron trifluoride |
| CN104209003A (en) * | 2014-08-16 | 2014-12-17 | 刘小秦 | Industrial production method for separating boron isotope product based on methyl-phenoxide-boron trifluoride complex |
| CN104230972A (en) * | 2014-08-16 | 2014-12-24 | 刘小秦 | Method for purifying anisole-boron trifluoride complex |
| CN104944432A (en) * | 2015-06-30 | 2015-09-30 | 莱芜亚赛陶瓷技术有限公司 | Superfine 10B-rich titanium diboride powder and preparation method thereof |
| CN105664718A (en) * | 2016-01-22 | 2016-06-15 | 渤海大学 | Method for isolating and producing enriched 28Si, 29Si and 30Si by serially connected multiple towers and apparatus used by method |
| CN105664718B (en) * | 2016-01-22 | 2018-03-20 | 渤海大学 | The production enrichment of multitower separation28Si、29Si and30Si methods and its used device |
| CN108275691B (en) * | 2018-04-13 | 2020-03-17 | 壹号元素（广州）科技有限公司 | Method and system for simultaneously producing high-concentration boron-10 boron trifluoride and high-concentration boron-11 boron trifluoride |
| CN108275691A (en) * | 2018-04-13 | 2018-07-13 | 壹号元素（广州）科技有限公司 | Method and system that are a kind of while producing -11 boron trifluoride of -10 boron trifluoride of highly concentrated boron and highly concentrated boron |
| CN110735208A (en) * | 2019-09-03 | 2020-01-31 | 刘禹超 | Industrial production method of neutron radiation protection fiber materials |
| RU2729797C1 (en) * | 2019-12-27 | 2020-08-12 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Российский химико-технологический университет имени Д.И. Менделеева" (РХТУ им. Д.И. Менделеева) | Mass transfer column |
| CN111389224A (en) * | 2020-03-30 | 2020-07-10 | 辽宁鸿昊化学工业股份有限公司 | Method for enriching boron-10 isotope anti-blocking tower by distillation method |
| CN111282438A (en) * | 2020-04-01 | 2020-06-16 | 辽宁鸿昊化学工业股份有限公司 | High abundance10B isotope enrichment method |
| CN111282438B (en) * | 2020-04-01 | 2023-08-22 | 辽宁鸿昊化学工业股份有限公司 | High abundance 10 B isotope enrichment method |
| CN113750797A (en) * | 2021-09-15 | 2021-12-07 | 黑龙江豪运药业有限公司 | Device and method for separating high-abundance isotope boron 11 boron trifluoride by low-temperature vacuum rectification boron trifluoride |
| CN115608156A (en) * | 2022-12-19 | 2023-01-17 | 淄博颐康环保科技有限公司 | Sectional type cooling complexing device and complexing method for separating boron isotopes |
| CN116688756A (en) * | 2023-08-03 | 2023-09-05 | 天津天和盛新材料科技有限公司 | Continuous production process method for separating boron isotopes |
| CN116688756B (en) * | 2023-08-03 | 2023-10-27 | 天津天和盛新材料科技有限公司 | Continuous production process method for separating boron isotopes |
| CN116832615A (en) * | 2023-08-29 | 2023-10-03 | 天津天和盛新材料科技有限公司 | Continuous production process method for silicon isotopes |
| CN116832615B (en) * | 2023-08-29 | 2023-11-21 | 天津天和盛新材料科技有限公司 | Continuous production process method for silicon isotopes |
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Application publication date: 20121114 |