CN214051168U - Energy-saving hydrogen isotope oxide separation system - Google Patents
Energy-saving hydrogen isotope oxide separation system Download PDFInfo
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- CN214051168U CN214051168U CN202022968769.6U CN202022968769U CN214051168U CN 214051168 U CN214051168 U CN 214051168U CN 202022968769 U CN202022968769 U CN 202022968769U CN 214051168 U CN214051168 U CN 214051168U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model discloses an energy-saving hydrogen isotope oxide separation system, including water purification unit, the first grade heat exchanger, the second grade heat exchanger, the rectifying column, the falling liquid film heat exchanger, a compressor, a condenser, the backward flow buffer tank, vapour and liquid separator, vacuum pump and refrigerating unit, in the rectification process with rectifying column top of the tower vapour through the pressurization intensification, carry out high-efficient heat transfer with the enrichment water at the bottom of the tower in the falling liquid film heat exchanger, utilize vapour condensation latent heat to provide the required heat of the evaporation of the enrichment water at the bottom of the tower, avoided the heat of the vapour at the top of the tower to be taken away by the cooling water and the enrichment water at the bottom of the tower additionally inputs a large amount of heats to evaporate the drawback, realized the apparent reduction of whole rectification separation energy consumption; meanwhile, through energy integration optimization, the raw material water is preheated by using the liquid with higher temperature output by the rectifying tower, and the energy utilization efficiency is further improved. The utility model discloses the flow is simple, device simple operation, system stability are good, can realize the reduction of rectification unit energy consumption 60 ~ 85%, have apparent engineering using value.
Description
Technical Field
The utility model relates to a hydrogen isotope separation technology field, specifically say, relate to an energy-saving hydrogen isotope oxide separation system.
Background
Protium (a)1H) And deuterium (2H or D) is two nuclides of hydrogen isotopes, and the separation process of protium deuterium oxide has an extremely important position in the fields of civilian use, nuclear power, fusion energy, military industry and the like.
Protium-deuterium separation system is the key technology for heavy water production and water deuterium removal. The natural water has a deuterium content of about 140 to 150ppm, and about 1 deuterium atom (the remainder being protium atoms) per 6600 hydrogen atoms. The pre-concentration of deuterium in water is a necessary step for heavy water production and is also a key link for determining the production cost of heavy water. As opposed to deuterium enrichment, the removal of deuterium from water results in water with a deuterium concentration lower than the natural concentration, the so-called deuterium depleted water or deuterium depleted water. Research shows that the application of deuterium-depleted water has the effects of improving the immunity of organisms, delaying senility, enhancing metabolism and the like, and has certain effects in the process of clinically and auxiliarily treating cancers such as lung cancer, cervical cancer, nasopharyngeal cancer, breast cancer, liver cancer and the like, so that the deuterium-depleted water has attracted extensive attention of researchers and people at present.
The separation method of the hydrogen isotope oxide mainly includes a chemical exchange method, a rectification method, an electrolysis method, a chromatographic separation method, a thermal diffusion method, a membrane diffusion adsorption method, a centrifugation method, a laser method, and the like. However, as a method for industrial production, methods having large-scale utility value mainly include a chemical exchange method, an electrolytic method, and a rectification method. The chemical exchange method realizes separation based on different distribution coefficients of hydrogen isotope oxides in each phase under different temperature conditions, such as a water-hydrogen double-temperature exchange method, but the method relates to multi-tower temperature change control, has complex operation and high equipment investment cost, and relates to corrosive hydrogen carriers such as hydrogen sulfide. The combination of catalytic exchange and electrolysis can significantly improve the separation efficiency, but the process uses a large amount of noble metal catalyst, the productivity is limited, and the power consumption investment is extremely high. The rectification method utilizes the difference of vapor pressures of different components to realize the separation purpose, although the vapor pressures of the components have very small difference and the balance driving force is small, large-scale treatment can be realized by increasing balance stages or cascade operation and other modes, and meanwhile, the method has the advantages of simple and reliable operation, no pollution in the production process, less fixed investment, low operation and maintenance cost and the like, thereby being concerned.
In the traditional rectification process, materials in a tower kettle are heated and vaporized; after vaporization, the mixture enters a rectifying tower to transfer mass and heat with a descending liquid phase material, and is vaporized and condensed continuously, so that the light and heavy components are distributed in two phases; the ascending vapor finally reaches the tower top to be condensed, part of the ascending vapor is extracted as a product, and part of the ascending vapor flows back to the tower. In the whole rectification process, most of heat is used for liquid phase boiling at the bottom of the tower and vapor condensation at the top of the tower, and the energy consumption corresponding to the phase change process is very high. The traditional rectification technology is mainly optimized by optimizing operation conditions, tower members, improving the performance of a reactive rectification catalyst and the like, but the improvement space is limited, and the energy-saving effect is not obvious.
SUMMERY OF THE UTILITY MODEL
To the problem that the separation energy consumption is high in the above-mentioned prior art, the utility model provides an energy-saving hydrogen isotope oxide piece-rate system.
In order to realize the purpose, the utility model discloses a technical scheme as follows:
an energy-saving separation system for hydrogen isotope oxide comprises a water purification unit, a primary heat exchanger, a secondary heat exchanger, a rectifying tower, a falling film heat exchanger, a compressor, a condenser, a reflux buffer tank, a gas-liquid separator, a vacuum pump and a refrigerating unit, wherein,
the water purification unit inputs external raw water through a raw water pipeline and carries out deep purification treatment;
the primary heat exchanger, the secondary heat exchanger and the rectifying tower are communicated through a liquid inlet pipeline, and purified raw material water is input into a specified feed inlet of the rectifying tower;
a gas-phase discharge port on the top of the rectifying tower is sequentially communicated with a compressor and the falling film heat exchanger through an independent gas-phase discharge pipeline and is used for pressurizing and heating dilution steam output from the top of the rectifying tower to form dilution compressed steam and exchanging heat in the falling film heat exchanger;
a liquid phase discharge port positioned at the bottom of the rectifying tower is respectively communicated with the primary heat exchanger and the falling film heat exchanger through independent liquid phase discharge pipelines, and is used for carrying out primary heat exchange and temperature rise on raw material water in the primary heat exchanger and carrying out heat exchange and evaporation with dilution compressed steam in the falling film heat exchanger;
the falling film heat exchanger is communicated with a designated steam inlet of the rectifying tower through an enriched water reflux pipeline and is used for returning an enriched water liquid phase to the rectifying tower after being evaporated, and the falling film heat exchanger is sequentially communicated with a secondary heat exchanger, a condenser and a reflux buffer tank through a condensation discharge pipeline and is used for inputting depleted liquid into the secondary heat exchanger to carry out secondary heat exchange and temperature rise on raw material water, condensing the depleted liquid in the condenser and reducing the temperature to the temperature of a material at the top of the rectifying tower and inputting the depleted liquid into the reflux buffer tank;
the reflux buffer tank is communicated with a specified reflux port at the top of the rectifying tower through a barren water reflux pipeline and is used for returning part of barren liquid to the rectifying tower; the reflux buffer tank is used for extracting a dilution end product through a dilution water discharging pipeline; the reflux buffer tank is sequentially connected with a gas-liquid separator and a vacuum pump through an emptying pipeline and is used for maintaining the required vacuum degree for the system;
the first-stage heat exchanger extracts the enriched water through an enriched water discharging pipeline;
the refrigerating unit is respectively communicated with the condenser, the vacuum pump and the compressor oil station through cooling pipelines and is used for providing required cooling media.
Furthermore, the bottom of the rectifying tower is provided with a reboiler which forms circulation with the rectifying tower, and the reboiler is used for providing heat energy for the rectifying tower in a start-up stage and is closed in a stable operation stage of the rectifying tower.
Furthermore, the refrigerating unit is also provided with a water reducing tower forming a circulation with the refrigerating unit, and the water reducing tower is used for reducing the temperature of the refrigerating unit.
Specifically, the rectifying tower is in a negative pressure state during operation, the pressure at the top of the tower is 6-15 kPa, and the operating temperature in the tower is lower than 65 ℃.
Specifically, cooling media required by the vacuum pump and the condenser are provided by a refrigerating unit, and the temperature of the media is 5-15 ℃.
Furthermore, a first flow controller is arranged on the raw water pipeline, a second flow controller is arranged on a liquid phase discharging pipeline between the rectifying tower and the primary heat exchanger, a third flow controller is arranged on a liquid phase discharging pipeline between the rectifying tower and the falling film heat exchanger, a fourth flow controller is arranged on the barren water backflow pipeline, and a fifth flow controller is arranged on the barren water discharging pipeline.
Further, the backflow buffer tank is communicated with the compressor through a cooling pipeline and used for cooling the compressor, and a sixth flow controller is arranged on the cooling pipeline.
The rectifying tower is provided with a plurality of temperature sensors, differential pressure sensors and pressure sensors; the gas-liquid separator is also provided with a pressure sensor; and a temperature sensor is also arranged on the backflow buffer tank.
Furthermore, the energy-saving hydrogen isotope oxide separation system also comprises a control system which is used for controlling all the components to automatically operate according to the set process.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) the utility model discloses it heaies up to pass through the pressurization with rectifying column top of the tower vapour, carry out the heat transfer with the enrichment water at the bottom of the tower in falling liquid film heat exchanger, utilize the vapour condensation latent heat to provide the required heat of the evaporation of the enrichment water at the bottom of the tower, avoided the top of the tower vapour heat to be taken away by the cooling water and the enrichment water at the bottom of the tower need additionally input a large amount of heats again and carry out the drawback of evaporating, whole process only needs to input a small amount of compressor electric energy and a small amount of vapour condensate recooling refrigeration, can realize showing the reduction of whole rectification separation process energy consumption. The utility model discloses simple, the device simple operation of flow, system stability are good, to the processing demand of different scales, can realize the reduction of rectification unit energy consumption 60 ~ 85%, and the processing scale is big more, and energy-conserving effect is more obvious. Therefore, the utility model discloses be expected to show the current situation that reduces hydrogen isotope oxide separation system separation cost height, have very showing engineering using value.
(2) The utility model discloses carry out twice preheating with the higher tower bottom enrichment water of temperature and barred liquid to former feed water respectively, promoted the feed temperature of former feed water, reduced the energy consumption that heats to the former feed water feeding and the feeding processing energy consumption of rectifying column, further reduced the whole energy consumption of system.
(3) The utility model adopts a negative pressure rectification process, controls the pressure at the top of the tower to be 6-15 kPa, and promotes the separation factor of the hydrogen isotope oxide to exceed 2%; meanwhile, under the negative pressure condition, the operation temperature in the tower is lower than 65 ℃, the heating requirement of the system is low, and the energy consumption is reduced.
Drawings
Fig. 1 is a schematic diagram of a system structure in an embodiment of the present invention.
In the drawings, the names of the parts corresponding to the reference numerals are as follows:
1-a water purification unit, 2-a primary heat exchanger, 3-a secondary heat exchanger, 4-a rectifying tower, 5-a falling film heat exchanger, 6-a compressor, 7-a condenser, 8-a reflux buffer tank, 9-a gas-liquid separator, 10-a vacuum pump, 11-a refrigerating unit, 12-a reboiler, 13-a raw water pipeline, 14-a liquid inlet pipeline, 15-a gas phase discharge pipeline, 16-a liquid phase discharge pipeline, 17-an enriched water reflux pipeline, 18-a condensation discharge pipeline, 19-a depleted water reflux pipeline, 20-a depleted water discharge pipeline, 21-an emptying pipeline, 22-a cooling pipeline, 23-an enriched water discharge pipeline, 24-a first flow controller, 25-a second flow controller and 26-a third flow controller, 27-fourth flow controller, 28-fifth flow controller, 29-sixth flow controller.
Detailed Description
The present invention will be further described with reference to the following drawings and examples, and embodiments of the present invention include, but are not limited to, the following examples.
Examples
As shown in fig. 1, the energy-saving separation system for hydrogen isotope oxide comprises a water purification unit 1, a primary heat exchanger 2, a secondary heat exchanger 3, a rectifying tower 4, a falling film heat exchanger 5, a compressor 6, a condenser 7, a reflux buffer tank 8, a gas-liquid separator 9, a vacuum pump 10, a refrigerating unit 11, a water-reducing tower and a reboiler 12, wherein,
the water purification unit receives external raw water through a raw water pipeline 13 and carries out deep purification treatment;
the primary heat exchanger, the secondary heat exchanger and the rectifying tower are communicated through a liquid inlet pipeline 14, and purified raw water is received by a specified feed inlet of the rectifying tower;
a gas-phase discharge port on the top of the rectifying tower is sequentially communicated with a compressor 6 and a falling film heat exchanger 5 through an independent gas-phase discharge pipeline 15, and is used for pressurizing and heating dilution steam output from the top of the rectifying tower to form dilution compressed steam and carrying out efficient heat exchange in the falling film heat exchanger;
a liquid phase discharge port positioned at the bottom of the rectifying tower is respectively communicated with the primary heat exchanger 2 and the falling film heat exchanger 5 through an independent liquid phase discharge pipeline 16, and is used for carrying out primary heat exchange and temperature rise on raw material water in the primary heat exchanger and carrying out heat exchange and evaporation with dilution compressed steam in the falling film heat exchanger;
the falling film heat exchanger is communicated with a designated steam inlet of the rectifying tower through an enriched water reflux pipeline 17 and is used for returning an enriched water liquid phase to the rectifying tower after being evaporated, and the falling film heat exchanger is sequentially communicated with a secondary heat exchanger, a condenser and a reflux buffer tank through a condensation discharge pipeline 18 and is used for inputting depleted liquid into the secondary heat exchanger to carry out secondary heat exchange and temperature rise on raw material water, condensing the depleted liquid in the condenser and cooling to the temperature of a material at the top of the rectifying tower and inputting the depleted liquid into the reflux buffer tank;
the reflux buffer tank is communicated with a specified reflux port at the top of the rectifying tower through a barren water reflux pipeline 19 and is used for returning part of barren liquid to the rectifying tower; the reflux buffer tank extracts a dilution end product through a dilution water discharge pipeline 20; the reflux buffer tank is sequentially connected with a gas-liquid separator and a vacuum pump through an emptying pipeline 21 and is used for maintaining the required vacuum degree for the system;
the first-stage heat exchanger extracts the enriched water through an enriched water discharging pipeline 23;
the refrigerating unit is respectively communicated with a condenser, a vacuum pump and a compressor oil station through a cooling pipeline 22 and used for providing required cooling media;
the reboiler is communicated with the bottom of the rectifying tower to form circulation and is used for providing heat energy for the rectifying tower in a start-up stage and closing the rectifying tower in a stable operation stage;
the cooling tower is communicated with the refrigerating unit and forms circulation for cooling the refrigerating unit.
The raw water pipeline is provided with a first flow controller 24, a second flow controller 25 is arranged on a liquid phase discharging pipeline between the rectifying tower and the primary heat exchanger, a third flow controller 26 is arranged on a liquid phase discharging pipeline between the rectifying tower and the falling film heat exchanger, a fourth flow controller 27 is arranged on a barren water backflow pipeline, and a fifth flow controller 28 is arranged on a barren water discharging pipeline. The backflow buffer tank is communicated with the compressor through a cooling pipeline and used for cooling the compressor, and a sixth flow controller 29 is arranged on the cooling pipeline.
In practical application, the utility model discloses entire system can realize full automatization operation through configuration control system, and this control system can adopt PLC or DCS control system to include the host computer, with the wired and/or wireless connection's of host computer lower computer etc.. A plurality of temperature sensors (such as T1-T4, the number of which can be adjusted according to the practical application condition), a differential pressure sensor (DP1) and a pressure sensor (P1) are arranged on the rectifying tower at equal intervals; the six flow controllers can selectively adopt modes of combining a variable frequency pump with a flow meter, combining an adjusting valve with the flow meter and the like to adjust the liquid flow, and the control of the flow controllers is realized through a control system; the compressor adopts a variable frequency compressor, and the output of the compressor is adjusted by measuring a pressure value P1 at the top of the rectifying tower through a control system, so that the pressure of the rectifying tower is kept stable; the first flow controller is used for adjusting the feed flow of raw water; the second flow controller is used for adjusting the flow of the enriched water extracted from the tower bottom and ensuring that the tower kettle has a specific liquid level; the third flow controller is used for adjusting the flow entering the falling film heat exchanger; the fourth flow controller is used for adjusting the backflow flow; the fifth flow controller is used for adjusting the flow of barren water extracted from the tower top; the sixth flow controller is used for adjusting the water flow for cooling the compressor; the flow of the fourth to sixth flow controllers is comprehensively adjusted by the control system, so that the liquid level in the reflux buffer tank is ensured to be maintained stably; the vacuum pump is used for adjusting and maintaining the system vacuum by measuring the pressure P2 of a pressure sensor arranged on the gas-liquid separator through the control system; the temperature T5 of the liquid in the return buffer tank (detected by a temperature sensor provided on the return buffer tank) ensures that the required value is maintained by the control system adjusting the flow or temperature of the cooling water provided by the refrigeration unit; manual valves are arranged at the positions of the whole system for maintenance, repair and the like, and electromagnetic valves or pneumatic valves are adopted for the rest parts, so that the full-automatic operation of the whole system is realized.
The implementation process of the energy-saving hydrogen isotope oxide separation system mainly comprises three sections of raw material water purification, rectification separation process and separation product treatment, and specifically comprises the following steps:
s10, purifying the raw water to remove impurities;
when the raw material water comes from a natural water source, the raw material water is sequentially subjected to sedimentation, primary filtration and deep purification after being taken, and the raw material water is subjected to industrial water purification technology, comprehensive fine filtration, adsorption, reverse osmosis and other technologies to form purified water as raw material water for rectification separation.
S20, rectifying and separating the purified raw material water, generating lean water at the top part based on the separation degree and the treatment requirement, and leading out the rich water at the bottom part:
s21, the purified raw material water is subjected to heat exchange and temperature rise through a primary heat exchanger and a secondary heat exchanger in sequence, and when the temperature of the purified raw material water reaches the temperature of a specified material, the purified raw material water is input into a rectifying tower from a specified feed inlet;
s22, forming ascending vapor and descending liquid in the rectifying tower by the raw material water, and carrying out hydrogen isotope exchange reaction on the surface of a filler in the rectifying tower to realize hydrogen isotope transfer, so that the content of heavy components in the ascending vapor is reduced to form depleted vapor at the tower top, and the content of heavy components in the descending liquid is lifted to form enriched water at the tower bottom;
s23, inputting enriched water with a set flow rate extracted from the tower bottom into a primary heat exchanger to serve as a primary heat exchange source for raw material water, inputting the rest of the enriched water into a falling film heat exchanger, performing efficient heat exchange with dilution compressed vapor which is output from the tower top and is formed by pressurization and temperature rise, evaporating the phase of the enriched water, and returning the evaporated enriched water to the rectifying tower from a specified vapor inlet to continue to perform hydrogen isotope exchange reaction;
s24, after heat exchange in the falling film heat exchanger, diluting compressed vapor is condensed into diluting liquid and then is input into a secondary heat exchanger as a secondary heat exchange source for raw material water, diluting liquid is primarily condensed, and is input into a condenser, and a cooling medium provided by a refrigerating unit is condensed and cooled to be consistent with the temperature of the material at the top of the rectifying tower, so that diluting condensed liquid is formed;
s25, inputting the depleted condensed liquid into a reflux buffer tank, extracting part of the depleted condensed liquid as a depleted end product according to a preset flow, and returning the rest of the depleted condensed liquid to the top of the rectifying tower according to a preset reflux proportion to continue to perform hydrogen isotope exchange reaction;
s26, adjusting the operation parameters of the rectification separation process to realize hydrogen isotope separation of different degrees and obtain depleted end products of different concentrations;
the vacuum degree required by the rectification separation process is maintained by a gas-liquid separator and a vacuum pump which are connected behind a reflux buffer tank, cooling media required by the vacuum pump and a condenser are provided by a refrigerating unit, the temperature of the media is 5-15 ℃, the rectification tower is in a negative pressure state during operation, the pressure at the top of the tower is 6-15 kPa, the separation factor of the hydrogen isotope oxide is increased by over 2%, the operation temperature in the tower is lower than 65 ℃, the heating requirement of the system is low, and the energy consumption is reduced.
Specifically, the rectifying tower is a core reactor in the separation process, and the filler in the tower adopts a metal filler with a coating formed by special treatment on the surface and used for improving the surface hydrophilicity. Compared with the traditional copper filler, the treatment efficiency can be higher, the cost of the material can be reduced by 75%, the slag falling problem of the filler can be obviously improved, and the parking maintenance requirement is reduced, so that the operation and maintenance cost of the system is reduced. Bulk packing is preferred for small scale applications and structured packing is preferred for large scale engineering applications.
In the process, the vapor at the top of the tower is compressed, pressurized and heated, enters a falling film heat exchanger to heat and vaporize the enriched water at the bottom of the tower, and then enters the bottom of the rectifying tower. The temperature of steam output from the tower top is raised by inputting a small amount of compression work, and the evaporation of water-enriched materials at the tower bottom is realized by utilizing the huge latent heat of the condensation process, so that the overall energy consumption can be obviously reduced by more than 60%. A falling film heat exchanger is selected as a device for exchanging heat between the steam output from the tower top and the enriched water output from the tower bottom, and relates to phase change of two-phase heat exchange media, and the device has higher heat transfer efficiency.
In the process, aiming at a non-tritium-involved system, such as a low deuterium water production process, the purified residual water of the water purification unit and the enriched water introduced from the bottom of the rectifying tower are used as a water replenishing source of a water descending tower of a refrigerating unit, so that the water utilization efficiency of the system is improved.
S31, carrying out post-separation treatment on the barren end product extracted from the reflux buffer tank to form barren water for output;
s32, carrying out post-separation treatment on the enriched water subjected to heat exchange and temperature reduction from the primary heat exchanger to form enriched water for output;
wherein, aiming at the separation system of the output product, such as the deuterium-depleted water preparation process, the produced deuterium-depleted water is sterilized, bottled and labeled to form the product for output; the enriched product can be stored in a centralized way or input into a next procedure for deep concentration or extraction.
Application test data:
based on the system and the process, the separation of the low deuterium oxide water with the annual output of 5000t/a @50ppm is carried out, and the evaporation heat load of the bottom liquid of the tower is 8000 kW. Table 1 compares the operating energy consumption profiles of three types of processes: respectively the utility model, the whole electricity utilization function (the electric heating evaporator) and the steam heat supply. Compare whole by the thermal traditional handicraft of electric energy supply, adopt the utility model discloses can reduce heating power from 8000kW to 1150kW, reduce 85% power consumption promptly. The operation cost is analyzed and calculated as the electricity price of 0.6 yuan/kWh and the steam price of 150 yuan/t, and the operation is carried out for 8000h per year. The process of the utility model is adopted for year heating and running cost of 552 ten thousand yuan, and the direct power consumption of 3840 ten thousand yuan; and the steam heating cost is 1680 ten thousand yuan, and the energy consumption cost of the utility model is reduced by 67 percent.
TABLE 1 energy consumption comparison of the present invention with the conventional process
| Item | The utility model discloses | Direct electricity utilization | Conventional steam |
| Reboiler heat duty kW | 8000 | 8000 | 8000 |
| Steam consumption t/h | 14 | ||
| Consumption of electric power kWh | 1150 | 8000 | |
| Heating operation energy consumption (Wanyuan/year) | 552 | 3840 | 1680 |
Based on the separation of the annual low deuterium of 5000t/a @50ppm, different degrees of separation of hydrogen and deuterium can be realized by adjusting the key process operation parameters, and low deuterium products with different concentrations can be prepared, as shown in table 2.
TABLE 2 ability of the present invention to prepare deuterium depleted water products of different concentrations
| Product type (ppm) | Small unitHourly capacity (L/h) | Annual capacity (ton) |
| 25 | 375 | 3000 |
| 50 | 675 | 5400 |
| 75 | 1025 | 8200 |
| 100 | 1400 | 11200 |
| 130 | 1875 | 15000 |
It can be seen that the utility model discloses can show and reduce rectification separation energy consumption cost, have apparent practical and spreading value in fields such as heavy water production and deuterium-depleted water preparation.
The above-mentioned embodiment is only the preferred embodiment of the present invention, and is not a limitation to the protection scope of the present invention, but all the changes made by adopting the design principle of the present invention and performing non-creative work on this basis should belong to the protection scope of the present invention.
Claims (9)
1. An energy-saving separation system for hydrogen isotope oxide, which is characterized by comprising a water purification unit, a primary heat exchanger, a secondary heat exchanger, a rectifying tower, a falling film heat exchanger, a compressor, a condenser, a reflux buffer tank, a gas-liquid separator, a vacuum pump and a refrigerating unit, wherein,
the water purification unit inputs external raw water through a raw water pipeline and carries out deep purification treatment;
the primary heat exchanger, the secondary heat exchanger and the rectifying tower are communicated through a liquid inlet pipeline, and purified raw material water is input into a specified feed inlet of the rectifying tower;
a gas-phase discharge port on the top of the rectifying tower is sequentially communicated with a compressor and the falling film heat exchanger through an independent gas-phase discharge pipeline and is used for pressurizing and heating dilution steam output from the top of the rectifying tower to form dilution compressed steam and exchanging heat in the falling film heat exchanger;
a liquid phase discharge port positioned at the bottom of the rectifying tower is respectively communicated with the primary heat exchanger and the falling film heat exchanger through independent liquid phase discharge pipelines, and is used for carrying out primary heat exchange and temperature rise on raw material water in the primary heat exchanger and carrying out heat exchange and evaporation with dilution compressed steam in the falling film heat exchanger;
the falling film heat exchanger is communicated with a designated steam inlet of the rectifying tower through an enriched water reflux pipeline and is used for returning an enriched water liquid phase to the rectifying tower after being evaporated, and the falling film heat exchanger is sequentially communicated with a secondary heat exchanger, a condenser and a reflux buffer tank through a condensation discharge pipeline and is used for inputting depleted liquid into the secondary heat exchanger to carry out secondary heat exchange and temperature rise on raw material water, condensing the depleted liquid in the condenser and reducing the temperature to the temperature of a material at the top of the rectifying tower and inputting the depleted liquid into the reflux buffer tank;
the reflux buffer tank is communicated with a specified reflux port at the top of the rectifying tower through a barren water reflux pipeline and is used for returning part of barren liquid to the rectifying tower; the reflux buffer tank is used for extracting a dilution end product through a dilution water discharging pipeline; the reflux buffer tank is sequentially connected with a gas-liquid separator and a vacuum pump through an emptying pipeline and is used for maintaining the required vacuum degree for the system;
the first-stage heat exchanger extracts the enriched water through an enriched water discharging pipeline;
the refrigerating unit is respectively communicated with the condenser, the vacuum pump and the compressor oil station through cooling pipelines and is used for providing required cooling media.
2. The energy-saving separation system for hydrogen isotope oxides in claim 1, wherein the bottom of the rectification column is provided with a reboiler forming a cycle therewith, and the reboiler is used for providing heat energy for the rectification column in a start-up stage and is closed in a stable operation stage of the rectification column.
3. The energy efficient oxyhydride separation system of claim 1, wherein the chiller unit is further configured with a cooling tower forming a cycle therewith for cooling the chiller unit.
4. The energy-saving separation system for hydrogen isotopes and oxides as claimed in claim 1, wherein the rectification column is under negative pressure during operation, the pressure at the top of the column is 6-15 kPa, and the operation temperature in the column is lower than 65 ℃.
5. The energy-saving separation system for hydrogen isotopes and oxides as claimed in claim 1, wherein the cooling medium required by the vacuum pump and the condenser is provided by a refrigerating unit, and the temperature of the medium is 5-15 ℃.
6. The energy-saving separation system for hydrogen isotopes of any one of claims 1 to 5, wherein a first flow controller is arranged on the raw water pipeline, a second flow controller is arranged on a liquid-phase discharge pipeline between the rectifying tower and the primary heat exchanger, a third flow controller is arranged on a liquid-phase discharge pipeline between the rectifying tower and the falling film heat exchanger, a fourth flow controller is arranged on the depleted water reflux pipeline, and a fifth flow controller is arranged on the depleted water discharge pipeline.
7. The energy-saving separation system for hydrogen isotopes and oxides as claimed in claim 6, wherein the reflux buffer tank is communicated with the compressor through a cooling pipeline for cooling the compressor, and a sixth flow controller is disposed on the cooling pipeline.
8. The energy-saving separation system for hydrogen isotopes and oxides according to claim 7, wherein a plurality of temperature sensors, pressure difference sensors and pressure sensors are arranged on the rectifying tower; the gas-liquid separator is also provided with a pressure sensor; and a temperature sensor is also arranged on the backflow buffer tank.
9. The energy efficient oxyhydrogen separation system according to claim 8, further comprising a control system for controlling the components to automatically operate according to a set process.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113735132A (en) * | 2021-09-15 | 2021-12-03 | 黑龙江豪运药业有限公司 | Device and method for producing various abundant boron 10 isotopes in one tower |
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2020
- 2020-12-10 CN CN202022968769.6U patent/CN214051168U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113735132A (en) * | 2021-09-15 | 2021-12-03 | 黑龙江豪运药业有限公司 | Device and method for producing various abundant boron 10 isotopes in one tower |
| CN113735132B (en) * | 2021-09-15 | 2022-05-17 | 黑龙江豪运药业有限公司 | Device and method for producing various abundant boron 10 isotopes in one tower |
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