CN201493052U - Isotope separating device producing ultra-light water intermittently - Google Patents
Isotope separating device producing ultra-light water intermittently Download PDFInfo
- Publication number
- CN201493052U CN201493052U CN2009202078310U CN200920207831U CN201493052U CN 201493052 U CN201493052 U CN 201493052U CN 2009202078310 U CN2009202078310 U CN 2009202078310U CN 200920207831 U CN200920207831 U CN 200920207831U CN 201493052 U CN201493052 U CN 201493052U
- Authority
- CN
- China
- Prior art keywords
- rectifying column
- tower
- water
- storage tank
- oxygen
- 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
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to an isotope separating device producing ultra-light water intermittently, which comprises a plurality of rectifying towers which are connected, wherein the tower top of the first rectifying tower is connected with a reflux liquid storage tank through a condenser, a reflux liquid storage tank is connected with the rectifying tower through a liquid transmission pump, the tower top of a secondary rectifying tower is connected with the lower portion of the first rectifying tower through the condenser, and the tower kettle of the first rectifying tower is connected with the tower top of the secondary rectifying tower. Compared with the prior art, the isotope separating device simultaneously and continuously separates heavy oxygen water and intermittently separates ultra-light water, can simultaneously produce various specifications of products through regulating technical parameters, and has the advantages of saving investment, lowering cost and having simple and easy operation and the like.
Description
Technical field
The utility model relates to the stable isotope separation technology field, relate more specifically to a kind of can be when continuously producing heavy oxygen water the isotopic separation device of Batch Process depleted water.
Background technology
The hydrone of occurring in nature is formed (H by 2 hydrogen atoms and 1 oxygen atom
2O), protium have protium (
1H), deuterium (
2H is D) two kinds of stable isotopes and tritium (
3H is T) a kind of radio isotope, natural abundance is respectively 99.985%, 0.015% (150ppm), the tritium natural abundance is extremely low less than part per billion; Oxygen element aerobic-16 (
16O), oxygen-17 (
17O), oxygen-18 (
18O) three kinds of stable isotopes, natural abundance is respectively 99.76%, 0.04%, 0.2%.Can constitute multiple stable isotope hydrone by two hydrogen atoms and an oxygen atom, they are present in the natural water in varing proportions.
Heavy oxygen water is meant the water that oxygen-18 element and ordinary hydrogen element constitute, be mainly used in the research of aspects such as organism metabolism, the control of medicine synthesis step, environmental science and hydrogeology, chemical chain characteristic and chemical reaction mechanism, can also be widely used in the nuclear medicine diagnostic technical field as nuclear medicine diagnosis reagent, especially PET (positron emission tomography) developer is synthetic.
Depleted water claims low deuterium-oxide or poor deuterium-oxide again, be meant that the abundance of deuterium in the water is lower than the water of natural abundance (150ppm), its English name is: Deuterium Depleted Water, abbreviate as: DDW is mainly used in the drinking water of diseases such as preparing high-purity protium gas, nuclear magnetic resonance solvent and anti-curing cancers and health care etc.
At present, the preparation method and the device thereof of heavy oxygen water mainly contain: water rectification method, cryogenic rectification method, chemical exchange method, thermal diffusion method etc., industrial production is based on the water rectification method.Wherein, the water rectification method is produced heavy oxygen water, is to be raw material with natural water, through multistage tower cascade (series connection or series/parallel) separated oxygen isotope, obtains the heavy oxygen aquatic products in the bottom of final stage cascade tower.
At present, the preparation method of depleted water had once reported two warm exchange processes of hydrogen sulfide and centrifugal separation.
When adopting the two warm exchange processes of hydrogen sulfide to produce depleted water, utilize the isotope exchange reaction between hydrogen sulfide and the water, adopt the mode of cold tower and thermal tower multi-stage cascade serial connection to realize separating of heavy hydrogen and superheavy hydrogen, liquid charging stock water enters from cold top of tower, flows through hot and cold exchange column from top to bottom; Gas material hydrogen sulfide adds between cold and hot tower, and in cold and hot tower circulating from bottom to top, in exchange column, form convection current with liquid material, heavy ends are shifted and are concentrated in liquid phase to liquid phase by Chemical Exchange in the cold tower, and the concentration of heavy ends reaches maximum in cold tower bottom liquid phase; The liquid material that has concentrated heavy ends when flowing through thermal tower again with up gas generation Chemical Exchange, heavy ends are shifted to gas phase again, the liquid phase material of discharging from thermal tower enters and promptly gets the manufactured goods that reduced heavy hydrogen content after degassing tower removes hydrogen sulfide.Resulting depleted water deuterium content is below 135ppm.
When adopting centrifugal separation to produce depleted water, adopt pyroreaction steam boiler, rectification under vacuum tower and high speed centrifugation separator to obtain depleted water, the pyroreaction steam boiler is communicated with by the liquid phase region of steam lead with rectification under vacuum tower bottom; The rectification under vacuum tower is from last and go up and to be vacuum buffer district, gas phase zone, liquid phase region and enrichment region; Gas phase zone and liquid phase region are equipped with copper corrugated plating; The rectification under vacuum tower is provided with vacuum governor; The enrichment region bottom of rectification under vacuum tower bottom is connected with the pyroreaction steam boiler by mozzle, to form circulation; The place, vacuum buffer district of rectification under vacuum top of tower is connected with the high speed centrifugation separator by gas conduit.Resulting depleted water deuterium content is below 135ppm.
At present, all do not adopt the isotopic separation device to separate heavy oxygen water and the relevant report of intermittently separating depleted water simultaneously continuously both at home and abroad, more do not have to obtain simultaneously the device of heavy oxygen water and specific concentrations depleted water.
Summary of the invention
The purpose of this utility model is exactly to provide a kind of isotopic separation device for preparing the Batch Process depleted water of depleted water and heavy oxygen water simultaneously for the defective that overcomes above-mentioned prior art existence.
The purpose of this utility model can be achieved through the following technical solutions: a kind of isotopic separation device of Batch Process depleted water, it is characterized in that, this device is connected to form by the multistage rectification tower, wherein, the cat head of first order rectifying column connects the backflow fluid reservoir by condenser, this backflow fluid reservoir connects first order rectifying column by liquid delivery pump, and the cat head of subordinate's rectifying column is by the bottom of condenser connection higher level rectifying column, and the tower still of higher level's rectifying column connects the cat head of subordinate's rectifying column.
Described multistage rectification tower comprise the 3-10 level.
The tower still of described multistage rectification tower is equipped with reboiler.
Described first order rectifying column connects the natural water storage tank.
Described backflow fluid reservoir connects the depleted water gatherer.
The tower still of the afterbody rectifying column of described multistage rectification tower connects heavy oxygen aquatic products gatherer.
Compared with prior art, the utility model adopts the isotopic separation device to separate heavy oxygen water simultaneously continuously and intermittently separates depleted water, with a covering device by regulating technological parameter production plurality of specifications simultaneously product, have reduce investment outlay, reduce cost, advantage such as easy to operation, emission with original production system changes the depleted water product into simultaneously, strengthen comprehensive utilization of resources, avoided the discharging of surplus liquid in original production, strengthen comprehensive utilization of water resources, strengthened the heavy oxygen water and the depleted water competitiveness of product in market.
Description of drawings
Fig. 1 is a schematic diagram of the present utility model.
Number in the figure is described as follows:
1. heavy oxygen water separation device
2. phegma storage tank
3. liquid delivery pump
S
0-natural water; S
1-condensate liquid; S
2-phegma; S
3The depleted water of-cat head extraction; S
4The heavy oxygen water of output at the bottom of the-Ta;
T
1-the first rectifying column; T
2-the second rectifying column; T
N-1-Di (n-1) level rectifying column; T
n-Di n level rectifying column; N is a positive integer;
E
1-the first condenser; E
3-the second condenser; E
2n-3-Di (n-1) level condenser; E
2n-1-Di n level condenser; N is a positive integer;
E
2-the first reboiler; E
4-the second reboiler; E
2n-2-Di (n-1) level reboiler; E
2n-Di n level reboiler; N is a positive integer;
Ellipsis is represented the rectifying column of cascades at different levels among the figure.
The specific embodiment
Design of the present utility model is as follows:
The technical solution adopted in the utility model is: utilize stable isotope crystal cut in process, the separated simultaneously and hydrogen isotope of hydrogen isotope in the water and oxygen isotope is than the segregative characteristic of oxygen isotope, by changing the operating condition of heavy oxygen water separation device, change the emission at first order rectifying column top in the aquatic product process of heavy oxygen into depleted water, output depleted water intermittently when continuously producing heavy oxygen water.Heavy oxygen water separation device 1 of the present utility model is generally by multistage (T
1～T
n, be generally 3～10 grades) and cascade rectifying column composition, the specific operation condition of employing heavy oxygen water separation device first order tower can the Batch Process D abundance be the depleted water of 0.2ppm～125ppm, the heavy oxygen of extraction simultaneously water.In this production process, the oxygen isotope in the water is constantly separated in cascade unit, and hydrogen isotope is also simultaneously separated, can obtain to be shelled light the water of heavy hydrogen at the top of first order tower, the bottom of afterbody tower has then the obtained enrichment water of heavy oxygen.Change heavy oxygen water separation device operating condition, can be when producing heavy oxygen water continuously, Batch Process depleted water product.
Below various piece of the present utility model is described in detail:
Cascade rectification device
Cascade rectification device of the present utility model is by multistage rectification tower (T
1)～(T
n) be formed by connecting, and n is the integer between 3～10.The series connection of rectifying column inter-stage, each grade rectifying column can be a tower, also can be composed in parallel by a plurality of towers, rectifying progression can be more than 10 grades.
Reflux operation
Described natural water raw material (S
0) in above-mentioned cascade rectification device (1), carry out following steps respectively:
(i) at multistage rectification tower (T
1)～(T
n) in carry out cascade rectifying, at described first order rectifying column (T
1) in carry out, partial reflux or zero reflux operation, thus at final stage rectifying column (T
n) the bottom obtain heavy oxygen aquatic products (S
4);
(ii) in described first order rectifying column (T1), carry out total reflux operation, thereby at first order rectifying column (T
1) the top obtain the depleted water (S of D abundance between 0.2ppm～125ppm
1), at final stage rectifying column (T
n) the bottom obtain heavy oxygen aquatic products (S
4).
Wherein, step (i) is the partial reflux step, and step (ii) is the infinite reflux step.
The tower pressure of described step (i), temperature, cascade flow, add heat, condensation number is not specifically limited, only otherwise goal of the invention of the present utility model is produced restriction to get final product.Its scope of selecting for use can be selected according to workshop manual or manufacturer's standard.
(ii) tower pressure, temperature, cascade flow of described step, add heat, condensation number is not specifically limited, only otherwise goal of the invention of the present utility model is produced restriction to get final product.Its scope of selecting for use can be selected according to workshop manual or manufacturer's standard.
Step (i) can be identical with step technological parameter (ii), also can be different.
The utility model has utilized the characteristic of cascade erratic process, obtains the required heavy oxygen water and the depleted water of specific concentrations by partial reflux step and the infinite reflux step that hockets.Particularly, be to derive by extensive experimental with to material balance and mass transport process, set up the related of heavy oxygen water cascade unit production operation parameter and depleted water product D abundance, and according to this association and according to required product adjusting technological parameter.Described related empirical equation is as follows:
In the formula:
X: the abundance of deuterium in the depleted water product, ppm;
X
0: raw material (S
0) in the abundance of deuterium, ppm;
H: output is the liquid measure in the phegma storage tank (2), kg;
H
0: the liquid holdup in the cascade unit, kg;
A: coefficient, relevant with the cascade unit separating power, when the theoretical cam curve of cascade unit reaches 2500～4000, A=180;
α: separation;
L: capacity of returns, kg/hr;
T: the time of Batch Process (being the total reflux operation time), hr.
By correlation (1) as can be known, the variation of D abundance is relevant with liquid holdup, theoretical cam curve, production operation industrial and mineral, output (being the liquid measure in the phegma storage tank), the production time (being infinite reflux running time) of cascade separator.Change the operating condition of heavy oxygen water separation device, first order rectifying column with the heavy oxygen water separation device, change total reflux operation into by original partial reflux, this moment, system did not have charging, cat head not to have emission, reflux stream is returned in the tower through the phegma storage tank, and in tower, hydrogen isotope in the water and oxygen isotope are simultaneously separated, the top area of first order tower obtain stripping light the depleted water of deuterium, the bottom section of afterbody tower obtains the heavy oxygen water of enriched in oxygen-18.For existing heavy oxygen water separation device, after the production operation industrial and mineral is determined,, can obtain the depleted water product of the different D abundances of 0.2ppm～125ppm scope by changing Batch Process time and output.
Light component (protium in the hydrogen isotope and the oxygen in the oxygen isotope-16) is constantly toward the cat head enrichment, heavy component (deuterium in the hydrogen isotope and the oxygen in the oxygen isotope-18) is constantly toward the enrichment of tower still, the water of can obtain enrichment at the top of first order rectifying column protium and oxygen-16 (
1H
2 16O), the water of the bottom of afterbody tower heavy hydrogen that then obtained enrichment and heavy oxygen (
2H
2 18O).Material in the phegma storage tank, increase along with the infinite reflux time, the abundance of deuterium constantly reduces, the speed that D abundance descends and the separative efficiency of separator, the production operation industrial and mineral, the time of staying of phegma in storage tank is relevant, for existing heavy oxygen water separation device, after the production operation industrial and mineral is determined, the time of staying of phegma in storage tank short more (being that liquid holdup is few more in the phegma storage tank), D abundance descends fast more in the phegma, by changing the infinite reflux running time and the time of staying of phegma in storage tank, can in the phegma storage tank, obtain the depleted water of the different D abundances of 0.2ppm～125ppm scope, according to the depleted water in demand extraction at the intermittence phegma storage tank of different D abundances.
The utility model adopts total reflux operation to prepare depleted water, irrelevant with the feed entrance point of heavy oxygen water separation device, and the theoretical cam curve that preparation heavy oxygen water needs is more than depleted water, and therefore every employing crystal heats up in a steamer the various separators that legal system is equipped with heavy oxygen water and all can adopt the utility model technology intermission to prepare depleted water.
Below in conjunction with specific embodiment, further illustrate the utility model.Should be understood that these embodiment only to be used to the utility model is described and be not used in the restriction scope of the present utility model.The experimental technique of unreceipted actual conditions in the following example, usually according to normal condition, or the condition of advising according to manufacturer.Ratio and percentage are based on weight, unless stated otherwise.
Unless otherwise defined or explanation, the meaning that all specialties used herein are familiar with scientific words and those skilled in the art is identical.Any in addition method similar or impartial to described content and material all can be applicable in the utility model method.
As shown in Figure 1, a kind of isotopic separation device of Batch Process depleted water, this device is formed by connecting (n is the integer between the 3-10) by n level rectifying column, wherein, first order rectifying column T
1Cat head by condenser E
1Connect backflow fluid reservoir 2, this backflow fluid reservoir 2 connects first order rectifying column T by liquid delivery pump 3
1, second level rectifying column T
2Cat head by condenser E
3Connect first order rectifying column T
1The bottom, first order rectifying column T
1The tower still is provided with reboiler E
2, first order rectifying column T
1The tower still connects second level rectifying column T
2Cat head, the rectifying column T of subordinate
nCat head by condenser E
2n-1Connect higher level's rectifying column T
N-1The bottom, higher level's rectifying column T
N-1The tower still connect the rectifying column T of subordinate
nCat head, the tower still of rectifying columns at different levels is equipped with reboiler, as second level rectifying column T
2The tower still be provided with reboiler E
4, n-1 level rectifying column T
N-1The tower still be provided with reboiler E
2n-2, n level rectifying column T
nThe tower still be provided with reboiler E
2nFirst order rectifying column T
1Connection natural water storage tank, natural water S
0Input first order rectifying column T from the natural water storage tank
1, backflow fluid reservoir 2 connects depleted water gatherer, depleted water S
3From 2 outputs of backflow fluid reservoir, afterbody rectifying Tata still connects heavy oxygen aquatic products S
4Gatherer.
The mode of production of heavy oxygen water is with natural water S
0Be raw material, enter heavy oxygen water separation device 1 first order rectifying column T
1, at first order rectifying column T
1The surplus liquid depleted water of top discharge heavy oxygen water S
3, at final stage rectifying column T
nThe bottom obtain heavy oxygen aquatic products S
4, producing in the process of heavy oxygen water first order rectifying column T continuously
1Finite reflux operation is (for S
0From the production technology that cat head enters first order rectifying column, first order rectifying column T
1Can not reflux), change first order rectifying column T
1Operating condition, keep the operating parameter (tower pressure, temperature, cascade flow, add heat, condensation number etc.) of rectifying columns at different levels constant, at first in phegma storage tank 2, add the natural water of certain design flow, stop first order rectifying column T then simultaneously
1Charging (S
0=0) and cat head extraction (S
3=0), with first order rectifying column T
1Change total reflux operation into by partial reflux, first order rectifying column T
1The condensate liquid S of cat head
1The phegma storage tank 2 of flowing through, with liquid delivery pump 3 with phegma S
2In the input tower, phegma S
2Flow and condensate liquid S
1Flow equate (S
1=S
2), in tower, hydrogen isotope in the water and oxygen isotope are simultaneously separated, light component (protium in the hydrogen isotope and the oxygen in the oxygen isotope-16) is constantly toward the cat head enrichment, heavy component (deuterium in the hydrogen isotope and the oxygen in the oxygen isotope-18) is constantly toward the enrichment of tower still, the water vapour of can obtain enrichment at the top of first order rectifying column protium and oxygen-16 is through condenser E
1Flow into phegma storage tank 2 (being depleted water) after the condensation, the water (being heavy oxygen water) of the bottom of afterbody tower has then obtained enrichment heavy hydrogen and heavy oxygen, material in the phegma storage tank 2, increase along with the infinite reflux time, the abundance of deuterium constantly reduces, the speed that D abundance descends is relevant with separative efficiency, production operation industrial and mineral, the time of staying of phegma in storage tank 2 of separator, regulates the abundance of deuterium according to following formula (1):
In the formula:
X: the abundance of deuterium in the depleted water product, ppm;
X
0: natural water raw material (S
0) in the abundance of deuterium, ppm;
H: output is the liquid measure in the phegma storage tank (2), kg;
H
0: the liquid holdup in the cascade rectification device, kg;
A: cascade rectification device separating power coefficient;
α: separation;
L: capacity of returns, kg/hr;
T: infinite reflux time, hr.
In another specific embodiment, above-mentioned change first order rectifying column (T
1) the operating condition process in, also can not be used in the phegma storage tank 2 and to inject a certain amount of natural water, but at first stop T
1Cat head extraction (the S of tower
3=0), the material in this moment phegma storage tank 2 constantly increases, and when reaching certain design flow, stops T again
1Charging (the S of tower
0=0), with T
1Tower changes total reflux operation into by partial reflux.
In another specific embodiment, heavy oxygen water separation device for prior art is transformed, after the production operation operating mode is determined, the time of staying of phegma in storage tank 2 is short more, D abundance descends fast more in the phegma, by changing infinite reflux running time (the infinite reflux time is preferred: 4 hours～400 hours) and the time of staying (time of staying preferred 0.5 hour～10 hour) of phegma in storage tank 2, can in phegma storage tank 2, obtain the depleted water of the different D abundances of 0.2ppm～125ppm scope, according to the depleted water in demand extraction at the intermittence phegma storage tank 2 of different D abundances.Repeat above-mentioned natural water S
0The operating process that charging is later, constantly Batch Process depleted water.
Described heavy oxygen water and depleted water are such outputs simultaneously:
Because heavy oxygen moisture is big from difficulty, the separator that the water rectification method prepares heavy oxygen water need reach 2500～4000 blocks of theoretical trays, usually form by 3～10 grades of rectifying column cascades (series connection or series/parallel), from being dosed into the time of producing the general needs of product is 5～10 months, therefore the aquatic product of heavy oxygen is continuous production, and the water rectification method prepares depleted water, than heavy oxygen moisture from easily, its separator generally needs 30～300 blocks of theoretical trays, utilize the crystal to heat up in a steamer the stalling characteristic of hydrogen isotope and oxygen isotope in the process, change the operating condition of heavy oxygen water separation device, first order rectifying column with the heavy oxygen water separation device, change total reflux operation into by original partial reflux, this moment, system did not have charging, cat head does not have emission, reflux stream is returned in the tower through the phegma storage tank, in tower, hydrogen isotope in the water and oxygen isotope are simultaneously separated, light component (protium in the hydrogen isotope and the oxygen in the oxygen isotope-16) is constantly toward the cat head enrichment, heavy component (deuterium in the hydrogen isotope and the oxygen in the oxygen isotope-18) is constantly toward the enrichment of tower still, the water of can obtain enrichment at the top of first order rectifying column protium and oxygen-16 (
1H
2 16O), the water of the bottom of afterbody tower heavy hydrogen that then obtained enrichment and heavy oxygen (
2H
2 18O).Material in the phegma storage tank, increase along with the infinite reflux time, the abundance of deuterium constantly reduces, the speed that D abundance descends and the separative efficiency of separator, the production operation industrial and mineral, the time of staying of phegma in storage tank is relevant, for existing heavy oxygen water separation device, after the production operation industrial and mineral is determined, the time of staying of phegma in storage tank short more (being that liquid holdup is few more in the phegma storage tank), D abundance descends fast more in the phegma, by changing the infinite reflux running time and the time of staying of phegma in storage tank, can in the phegma storage tank, obtain the depleted water of the different D abundances of 0.2ppm～125ppm scope, according to the depleted water in demand extraction at the intermittence phegma storage tank of different D abundances.
A kind of isotopic separation device of Batch Process depleted water, this device is formed by connecting by 3 grades of rectifying columns, wherein, the cat head of first order rectifying column connects the backflow fluid reservoir by condenser, this backflow fluid reservoir connects first order rectifying column by liquid delivery pump, the cat head of second level rectifying column connects the bottom of first order rectifying column by condenser, the tower still of first order rectifying column connects second level rectifying column cat head, the cat head of third level rectifying column is by the bottom of condenser connection second level rectifying column, and the tower still of second level rectifying column connects third level rectifying column cat head.
With natural water is raw material, D abundance 150ppm, flow with 250kg/hr enters first order rectifying column, the operating reflux ratio of first order rectifying column is 1,2500 of the theoretical cam curves of heavy oxygen water separation device, the operating pressure of rectifying columns at different levels is 120mmHg (absolute pressure), 50 ℃～52 ℃ of tower top temperatures, final stage rectifier bottoms heavy oxygen aquatic products produced quantity is 5g/hr, the natural water that in the phegma storage tank, adds, make the material total amount in the storage tank reach 1000kg, stop the charging and the cat head extraction of first order rectifying column then simultaneously, change first order rectifying column into total reflux operation by partial reflux, the condensate stream at first order rectifying column top is imported phegma in the tower with liquid delivery pump through the phegma storage tank, the flow of phegma equates with the flow of overhead condensation liquid, the time of staying of material is 2hr in this moment phegma storage tank, and control infinite reflux running time is 200hr, and the D abundance of depleted water is 2ppm in the phegma storage tank.
The quantum of output 5 gram/hr of heavy oxygen water, oxygen-18 abundance is greater than 95%.
A kind of isotopic separation device of Batch Process depleted water, this device is formed by connecting by 10 grades of rectifying columns, wherein, the cat head of first order rectifying column connects the backflow fluid reservoir by condenser, this backflow fluid reservoir connects first order rectifying column by liquid delivery pump, the cat head of subordinate's rectifying column is by the bottom of condenser connection higher level rectifying column, and the tower still of higher level's rectifying column connects subordinate's rectifying column cat head.
With natural water is raw material, D abundance 150ppm, flow with 250kg/hr enters first order rectifying column from cat head, 2500 of the theoretical cam curves of heavy oxygen water separation device, the operating pressure of rectifying columns at different levels is 70mmHg (absolute pressure), 40 ℃～42 ℃ of tower top temperatures, final stage rectifier bottoms heavy oxygen aquatic products produced quantity is 2.8g/hr, in the phegma storage tank, add natural water, make the inventory in the storage tank reach 500kg, stop the charging and the cat head extraction of first order rectifying column then simultaneously, change first order rectifying column into total reflux operation, the condensate stream at first order rectifying column top is through the phegma storage tank, with liquid delivery pump phegma is imported in the tower, the flow of phegma equates that with the flow of overhead condensation liquid the time of staying of material is 2hr in the phegma storage tank at this moment, control infinite reflux running time is 400hr, and the D abundance of depleted water is 0.2ppm in the phegma storage tank.
The quantum of output 2.2 gram/hr of heavy oxygen water, oxygen-18 abundance is greater than 95%.
Embodiment 4
A kind of isotopic separation device of Batch Process depleted water, this device is formed by connecting by 5 grades of rectifying columns, wherein, the cat head of first order rectifying column connects the backflow fluid reservoir by condenser, this backflow fluid reservoir connects first order rectifying column by liquid delivery pump, the cat head of subordinate's rectifying column is by the bottom of condenser connection higher level rectifying column, and the tower still of higher level's rectifying column connects subordinate's rectifying column cat head.
With natural water is raw material, D abundance 150ppm, flow with 500kg/hr enters first order rectifying column from cat head, 4000 of the theoretical cam curves of heavy oxygen water separation device, the operating pressure of rectifying columns at different levels is 120mmHg (absolute pressure), 50 ℃～52 ℃ of tower top temperatures, final stage rectifier bottoms heavy oxygen aquatic products produced quantity is 7.2g/hr, in the phegma storage tank, add natural water, make the inventory in the storage tank reach 500kg, stop the charging and the cat head extraction of first order rectifying column then simultaneously, change first order rectifying column into total reflux operation, the condensate stream at first order rectifying column top is through the phegma storage tank, with liquid delivery pump phegma is imported in the tower, the flow of phegma equates that with the flow of overhead condensation liquid the time of staying of material is 1hr in the phegma storage tank at this moment, control infinite reflux running time is 24hr, and the D abundance of depleted water is 50ppm in the phegma storage tank.
The quantum of output 4.8 gram/hr of heavy oxygen water, oxygen-18 abundance is greater than 98%.
Embodiment 5
With natural water is raw material, D abundance 150ppm, flow with 100kg/hr enters first order rectifying column, the operating reflux ratio of first order rectifying column is 4,4000 of the theoretical cam curves of heavy oxygen water separation device, the operating pressure of rectifying columns at different levels is 100mmHg (absolute pressure), 46 ℃～48 ℃ of tower top temperatures, final stage rectifier bottoms heavy oxygen aquatic products produced quantity is 6g/hr, the natural water that in the phegma storage tank, adds, make the material total amount in the storage tank reach 4000kg, stop the charging and the cat head extraction of first order rectifying column then simultaneously, change first order rectifying column into total reflux operation by partial reflux, the condensate stream at first order rectifying column top is imported phegma in the tower with liquid delivery pump through the phegma storage tank, the flow of phegma equates with the flow of overhead condensation liquid, the time of staying of material is 8hr in this moment phegma storage tank, and control infinite reflux running time is 100hr, and the D abundance of depleted water is 85ppm in the phegma storage tank.
The quantum of output 4.7 gram/hr of heavy oxygen water, oxygen-18 abundance is greater than 98%.
Embodiment 6
With natural water is raw material, D abundance 150ppm, flow with 500kg/hr enters first order rectifying column from cat head, 4000 of the theoretical cam curves of heavy oxygen water separation device, the operating pressure of rectifying columns at different levels is 760mmHg (absolute pressure), 100 ℃ of tower top temperatures, final stage rectifier bottoms heavy oxygen aquatic products produced quantity is 7.2g/hr, in the phegma storage tank, add natural water, make the inventory in the storage tank reach 1000kg, stop the charging and the cat head extraction of first order rectifying column then simultaneously, change first order rectifying column into total reflux operation, the condensate stream at first order rectifying column top is through the phegma storage tank, with liquid delivery pump phegma is imported in the tower, the flow of phegma equates that with the flow of overhead condensation liquid the time of staying of material is 2hr in the phegma storage tank at this moment, control infinite reflux running time is 36hr, and the D abundance of depleted water is 105ppm in the phegma storage tank.
The quantum of output 10 gram/hr of heavy oxygen water, oxygen-18 abundance is greater than 50%.
All quote in this application as a reference at all documents that the utility model is mentioned, just quoted as a reference separately as each piece document.Should be understood that in addition after having read foregoing of the present utility model, those skilled in the art can make various changes or modifications the utility model, these equivalent form of values fall within the application's appended claims institute restricted portion equally.
Claims (6)
1. the isotopic separation device of a Batch Process depleted water, it is characterized in that, this device is connected to form by the multistage rectification tower, wherein, the cat head of first order rectifying column connects the backflow fluid reservoir by condenser, this backflow fluid reservoir connects first order rectifying column by liquid delivery pump, and the cat head of subordinate's rectifying column is by the bottom of condenser connection higher level rectifying column, and the tower still of higher level's rectifying column connects the cat head of subordinate's rectifying column.
2. the isotopic separation device of a kind of Batch Process depleted water according to claim 1 is characterized in that, described multistage rectification tower comprises the 3-10 level.
3. the isotopic separation device of a kind of Batch Process depleted water according to claim 1 is characterized in that, the tower still of described multistage rectification tower is equipped with reboiler.
4. the isotopic separation device of a kind of Batch Process depleted water according to claim 1 is characterized in that, described first order rectifying column connects the natural water storage tank.
5. the isotopic separation device of a kind of Batch Process depleted water according to claim 1 is characterized in that, described backflow fluid reservoir connects the depleted water gatherer.
6. the isotopic separation device of a kind of Batch Process depleted water according to claim 1 is characterized in that, the tower still of the afterbody rectifying column of described multistage rectification tower connects heavy oxygen aquatic products gatherer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202078310U CN201493052U (en) | 2009-08-13 | 2009-08-13 | Isotope separating device producing ultra-light water intermittently |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202078310U CN201493052U (en) | 2009-08-13 | 2009-08-13 | Isotope separating device producing ultra-light water intermittently |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201493052U true CN201493052U (en) | 2010-06-02 |
Family
ID=42436262
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202078310U Expired - Fee Related CN201493052U (en) | 2009-08-13 | 2009-08-13 | Isotope separating device producing ultra-light water intermittently |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201493052U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105399165A (en) * | 2015-12-16 | 2016-03-16 | 高明 | Multi-stage series continuous rectification separation apparatus for light hydrogen molecular water and method |
| CN107530627A (en) * | 2015-03-31 | 2018-01-02 | 国立大学法人信州大学 | The manufacture method of the manufacture method of low deuterium-oxide, the separation method of heavy water and light-water and deuterium condensed water |
| CN107684828A (en) * | 2017-10-20 | 2018-02-13 | 江苏华益科技有限公司 | A kind of rectifier unit of high pure oxygen 16 |
| WO2022138162A1 (en) * | 2020-12-24 | 2022-06-30 | 大陽日酸株式会社 | Stable isotope enrichment device and stable isotope enrichment method |
-
2009
- 2009-08-13 CN CN2009202078310U patent/CN201493052U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107530627A (en) * | 2015-03-31 | 2018-01-02 | 国立大学法人信州大学 | The manufacture method of the manufacture method of low deuterium-oxide, the separation method of heavy water and light-water and deuterium condensed water |
| CN107530627B (en) * | 2015-03-31 | 2019-07-09 | 国立大学法人信州大学 | The manufacturing method and heavy water of low deuterium-oxide and deuterium condensed water and the separation method of light-water |
| US10471389B2 (en) | 2015-03-31 | 2019-11-12 | Shinsu University | Method for producing deuterium depleted water, method for separating heavy water and light water, and method for producing deuterium concentrated water |
| CN105399165A (en) * | 2015-12-16 | 2016-03-16 | 高明 | Multi-stage series continuous rectification separation apparatus for light hydrogen molecular water and method |
| CN107684828A (en) * | 2017-10-20 | 2018-02-13 | 江苏华益科技有限公司 | A kind of rectifier unit of high pure oxygen 16 |
| WO2022138162A1 (en) * | 2020-12-24 | 2022-06-30 | 大陽日酸株式会社 | Stable isotope enrichment device and stable isotope enrichment method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101597031B (en) | Method for intermittently producing deuterium depleted water through heavy-oxygen-enriched water separation device and device thereof | |
| CN201493052U (en) | Isotope separating device producing ultra-light water intermittently | |
| CN103601152B (en) | Method and apparatus for intermittent production of hyperpure 16O water during vacuum cascade rectification of heavy-oxygen water | |
| CN105399165B (en) | Plural serial stage continuous rectification detaches the device and method of light hydrogen molecular water | |
| CN105749575B (en) | The divided-wall distillation column of tail gas absorption liquid and condensate liquid recovery in production of polysilicon, method, processing system | |
| CN101148252B (en) | Method for preparing high purity oxygen by double-tower low temperature rectification | |
| CN103402919B (en) | Manufacture the integration method of ammonium nitrate | |
| CN103055697A (en) | Method and device for concentrating and enriching stable isotopes 2H, 18O and 13C | |
| CN104474898B (en) | Produce high abundance13C cryogenic rectification multitower cascade energy saver | |
| CN107073353A (en) | The improvement related to oxirane recovery | |
| CN105061187A (en) | A process for continuously producing m-toluic acid | |
| CN101985349A (en) | Production method for preparing deuterium depleted water | |
| CN101502758A (en) | Method for separating boron-10 isotopic element using reducing tower | |
| CN201553609U (en) | Sulfuric acid purifying device | |
| CN102730719B (en) | Industrial ammonia continuous purification apparatus and technology | |
| CN102030335B (en) | Method and device for removing boron impurity in chlorosilane system by rectification through double-tower thermocouple reaction | |
| CN115608156A (en) | Sectional type cooling complexing device and complexing method for separating boron isotopes | |
| CN106365178A (en) | Method for purification of hydrocyanic acid | |
| CN100369875C (en) | Device for separating 2-methyl butanol, 3-methyl butanol from iso amyl alcohol and its application method | |
| CN202470618U (en) | Preparation device for separating argon and oxygen through structured filler rectification | |
| CN214051168U (en) | Energy-saving hydrogen isotope oxide separation system | |
| CN112957762A (en) | System and method for rectifying and purifying methanol containing aldehyde in industrial pentaerythritol production | |
| CN102258878A (en) | Energy-saving device for producing <18>O-containing water by natural water | |
| CN102942539A (en) | Epoxy propane recovery and purification process | |
| CN101293635B (en) | Method for producing O18 water and deuterium deficient water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI LIANHONG ISOTOPE TECHNOLOGY CO., LTD. Effective date: 20121101 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20121101 Address after: 200062 Shanghai city Putuo District Yunling Road No. 345 Patentee after: Shanghai Research Institute of Chemical Industry Patentee after: Shanghai Lianhong Isotope Technology Co., Ltd. Address before: 200062 Shanghai city Putuo District Yunling Road No. 345 Patentee before: Shanghai Research Institute of Chemical Industry |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100602 Termination date: 20160813 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |