CN214158564U - Deuterium-depleted water preparation device - Google Patents
Deuterium-depleted water preparation device Download PDFInfo
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- CN214158564U CN214158564U CN202023295034.8U CN202023295034U CN214158564U CN 214158564 U CN214158564 U CN 214158564U CN 202023295034 U CN202023295034 U CN 202023295034U CN 214158564 U CN214158564 U CN 214158564U
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Abstract
The utility model discloses a deuterium-depleted water preparation facilities, gas-liquid separation device one end is through first heating device intercommunication heat transfer piece one end, heat transfer piece other end intercommunication gas-liquid separation device, the gas-liquid separation device other end and second heating device intercommunication and not communicate with heat transfer piece, come from gas-liquid separation device and be located the outer material of heat transfer piece and carry out the heat exchange with the material in the heat transfer piece in the second heating device. The utility model provides a deuterium-depleted water preparation facilities, the material that flows from gas-liquid separation device top need not cooling operation, can directly compress the heat source as follow-up material heating after rising temperature and boosting, realize energy reuse, the material that flows from gas-liquid separation device bottom can directly be extracted or flow back to gas-liquid separation device, carry out the heat exchange that circulates, deuterium-depleted water yield improves greatly, basically, it does not have the feeding loss to reach, solve the industry and enlarge and the high shortcoming of energy consumption, realize the production target of nearly zero energy consumption high output, deuterium-depleted water or distilled water can be prepared.
Description
Technical Field
The utility model belongs to the technical field of deuterium-depleted water or distilled water preparation, concretely relates to deuterium-depleted water preparation facilities.
Background
Deuterium-depleted water is water with deuterium content lower than that of natural water (natural deuterium content is generally 150-155ppm), especially water with deuterium content less than 135 ppm. In the area with higher altitude in nature, the deuterium content is slightly reduced, but the deuterium content is generally reduced little.
At present, many researches show that the deuterium-depleted water has obvious effects in the fields of tumor adjuvant therapy, nervous system disease improvement, immunity improvement and the like, and is one of the hot spots of the current researches. But the production cost of the deuterium-depleted water is high, and the deuterium-depleted water becomes one of the key factors restricting the large-scale popularization of the deuterium-depleted water.
At present, the production mode of deuterium-depleted water includes a low-temperature water rectification method, a chemical exchange method, an electrolysis method and the like. The chemical exchange method and the electrolytic method have relatively high separation factors, but the process uses flammable and explosive materials such as hydrogen, and has certain safety risks and the characteristic of difficult industrial amplification. At present, the most common method in large-scale production is low-temperature water rectification.
The water rectification method uses natural water as a raw material, and water is separated under the negative pressure condition generally. The traditional technology comprises the following main process flows:
1. after the material enters the rectifying tower, the material is evaporated by a reboiler 1 arranged at the bottom of the rectifying tower; the common heating mode is steam heating or electric heating, natural gas heating and the like;
2. the evaporated material is cooled by a condenser 2 arranged at the top of the rectifying tower and then is converted into a liquid phase from a gas phase, and most of the material flows back into the rectifying tower to form a rectifying process;
3. extracting a small part of materials from the top of the rectifying tower to form a top discharge material, namely a deuterium-depleted water product; while withdrawing a portion of the relatively heavier bottoms (deuterium content greater than the feed) from the bottom of the rectifier as shown in figure 1.
The separation process is clean and safe in material use and easy for industrial amplification. However, because of the relatively large reflux ratio required in the deuterium depleted water rectification production, several tons to tens of tons of industrial steam are required for producing one ton of deuterium depleted water, and the energy consumption is high.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems in the prior art, the present invention is directed to a deuterium-depleted water preparing apparatus.
In order to realize the above purpose, reach above-mentioned technological effect, the utility model discloses a technical scheme be:
the utility model provides a deuterium-depleted water preparation facilities, includes gas-liquid separation device, first heating device and second heating device, gas-liquid separation device one end communicates to the built-in heat transfer spare one end of second heating device through first heating device, and the heat transfer spare other end communicates gas-liquid separation device, and the gas-liquid separation device other end communicates with the inside intercommunication of second heating device and not communicate with the heat transfer spare, and the temperature of the material in the heat transfer spare is greater than the temperature of the material that gas-liquid separation device top and bottom flowed out, comes from gas-liquid separation device and is located the material of heat transfer spare outside and exchanges heat with the material in the heat transfer spare in the second heating device.
Furthermore, the top of the gas-liquid separation device is communicated to one end of the heat exchange piece through the first heating device, the other end, opposite to the heat exchange piece, of the gas-liquid separation device is communicated with the top of the gas-liquid separation device, and the bottom of the gas-liquid separation device is communicated with the inside of the second heating device and is not communicated with the heat exchange piece.
Further, still include the third heating device of a plurality of intercommunication, the built-in crooked heat exchange tube of third heating device, heat transfer one end communicates to the gas-liquid separation device top through first heating device, and the heat transfer other end selectivity communicates the gas-liquid separation device top through the crooked heat exchange tube in zero or one of them third heating device, the gas-liquid separation device bottom is communicated with the inside of second heating device and not with the heat transfer piece all the way, and another way selectivity of gas-liquid separation device bottom communicates with the crooked heat exchange tube in zero or one of them third heating device, and the feeding that just is located the outside heat exchange tube of crooked heat exchange tube in the third heating device enters into gas-liquid separation device after carrying out the heat exchange with the material in the crooked heat exchange tube.
Furthermore, the third heating device is a heat exchanger, and a bent heat exchange tube arranged in the third heating device is W-shaped.
Further, a material conveying device is arranged between the gas-liquid separation device and the second heating device, and the material conveying device is a conveying pump.
Further, the ratio of the reflux quantity of the gas-liquid separation device to the top discharge flow is 0: 1-1000: 1, the ratio of the top discharge flow to the feed flow is 0.01:1-1:1, the deuterium content in the top discharge is 0.01-150 ppm.
Furthermore, the gas-liquid separation device is provided with a plurality of gas-liquid separation devices which are communicated in parallel or in series.
Further, the gas-liquid separation device is a rectifying tower, the first heating device is a steam compression pump, the second heating device is a reboiler, and the heat exchange piece is W-shaped.
The utility model discloses a deuterium-depleted water preparation method adopts a deuterium-depleted water preparation facilities preparation to obtain deuterium-depleted water or distilled water, including following step:
feeding the material into a gas-liquid separation device for rectification operation, feeding the gas-phase material flowing out of the top of the gas-liquid separation device into a first heating device for heating and pressurizing operation, and then feeding the gas-phase material into a heat exchange piece arranged in a second heating device;
the material that flows out from the gas-liquid separation device bottom is taken out from the gas-liquid separation device bottom with the form of bottom ejection of compact all the way, the selectivity flows back to gas-liquid separation device after carrying out heat treatment, another way of material that flows out from the gas-liquid separation device bottom gets into inside the second heating device and with the material contactless in the heat transfer piece, use the material in the heat transfer piece as the heat source, the material that comes from gas-liquid separation device and is located the outside of heat transfer piece exchanges heat with the material in the heat transfer piece in the second heating device, the material in the heat transfer piece is cooled down and flows back to the gas-liquid separation device top, the outside material of heat transfer piece is heated and flows back to the gas-liquid separation device bottom, produce required low deuterium water or distilled water at the gas-liquid separation device top, the ratio of gas-liquid separation device's backward flow volume and top ejection of compact flow is 0: 1-1000: 1.
the utility model discloses an application of deuterium-depleted water or distilled water that deuterium-depleted water preparation method preparation obtained in the material of preparation deuterium-depleted hydrogen water, deuterium-depleted bubble water, deuterium-depleted normal saline and containing deuterium-depleted water or distilled water.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model discloses a deuterium-depleted water preparation facilities, deuterium-depleted water preparation facilities includes gas-liquid separation device, first heating device and second heating device, gas-liquid separation device one end communicates to the built-in heat transfer piece one end of second heating device through first heating device, heat transfer piece other end intercommunication gas-liquid separation device, the gas-liquid separation device other end just does not communicate with the heat transfer piece with the inside intercommunication of second heating device, the temperature of the material in the heat transfer piece is greater than the temperature of the material that gas-liquid separation device top and bottom flowed, the material that comes from gas-liquid separation device and be located the outside material of heat transfer piece and heat transfer piece carries out the heat exchange in the second heating device. The utility model provides a deuterium-depleted water preparation facilities, the material that flows out from gas-liquid separation device or rectifying column top need not to carry out cooling operation through the condenser, can directly compress heat source as follow-up material heating after rising temperature and boosting pressure, realize energy reuse, the material that flows out from gas-liquid separation device or rectifying column bottom can directly be extracted or flow back to gas-liquid separation device or rectifying column, carry out the heat exchange that circulates, deuterium-depleted water yield greatly improves, basically reach no feeding loss, when solving the industry amplification problem, also solve the shortcoming that the energy consumption is high, can realize the production target of nearly zero energy consumption high output, can realize the production target of preparing different quality of water through controlling the reflux ratio of gas-liquid separation device, prepare deuterium-depleted water when having the backward flow, need not to flow back and can be applied to the production of distilled water when the reflux ratio is 0, can obtain the distilled water or cool boiled water that purity is high and accord with the drinking water standard, the machine has multiple functions and great industrial application value.
Drawings
FIG. 1 is a schematic diagram of a prior art structure;
FIG. 2 is a schematic structural view of the present invention;
FIG. 3 is a position diagram of the transfer pump of the present invention;
fig. 4 is a schematic structural diagram of embodiment 1 of the present invention;
fig. 5 is a schematic structural diagram of embodiment 2 of the present invention;
fig. 6 is a schematic structural view of embodiment 3 of the present invention;
wherein, 1-reboiler; 2-a condenser; 3-a rectifying tower; 4-a vapor compression pump; 5, heat exchange tubes; 6-a heat exchanger; 7-a delivery pump; 8-bending the heat exchange tube.
Detailed Description
The embodiments of the present invention are described in detail below to make the advantages and features of the present invention easier to understand by those skilled in the art, thereby making more clear and definite definitions of the protection scope of the present invention.
As shown in fig. 2-6, a deuterium depleted water preparation device comprises a gas-liquid separation device, a first heating device and a second heating device, wherein one end of the gas-liquid separation device is communicated with one end of a heat exchange piece arranged in the second heating device through the first heating device, the other end of the heat exchange piece is communicated with the gas-liquid separation device for realizing the backflow of materials in the heat exchange piece, the bottom of the gas-liquid separation device is communicated with the inside of the second heating device and is not communicated with the heat exchange piece, the temperature of the materials in the heat exchange piece is higher than that of the materials flowing out of the top and the bottom of the gas-liquid separation device, the materials from the gas-liquid separation device and positioned outside the heat exchange piece exchange heat with the materials in the heat exchange piece in the second heating device, the materials in the heat exchange piece can be cooled and then flow back into the gas-liquid separation device, and the materials from the gas-liquid separation device and positioned outside the heat exchange piece are heated and then flow back into the gas-liquid separation device, the material entering the gas-liquid separation device and reflowing and the material in the gas-liquid separation device are subjected to isotope exchange and separation processes, so that deuterium-depleted water is generated at the top of the gas-liquid separation device, and water with deuterium content higher than that of natural concentration is generated at the bottom of the gas-liquid separation device.
As a specific implementation mode, the utility model discloses a deuterium depleted water preparation facilities still can set up zero, one or more third heating device according to the actual demand, and a plurality of third heating device intercommunication and liquid separator is ventilated to the parallel connection, and third heating device is heat exchanger 6, the built-in crooked heat exchange tube 8 of third heating device, and the built-in crooked heat exchange tube 8 of third heating device is the W type. One end (top) of the heat exchange piece is communicated to the top of the gas-liquid separation device through the first heating device, the other end (bottom) opposite to the heat exchange piece can be selectively communicated to the top of the gas-liquid separation device through zero or one of the bent heat exchange tubes 8 arranged in the third heating device, one way of the bottom of the gas-liquid separation device is communicated with the inside of the second heating device and is not communicated with the heat exchange piece, the other way of the bottom of the gas-liquid separation device can be communicated with the bent heat exchange tubes 8 arranged in zero or one of the third heating devices and is communicated to the outside, and the feeding inside the third heating device and the material inside the bent heat exchange tubes 8 arranged outside the bent heat exchange tubes 8 exchange heat.
As a specific embodiment, a material conveying device may be selectively disposed between the gas-liquid separation device and the second heating device, and the material conveying device is a conveying pump 7, as shown in fig. 3.
As a specific implementation manner, the deuterium depleted water preparing apparatus of the present invention may further include one or more gas-liquid separating devices according to actual requirements, wherein the plurality of gas-liquid separating devices are connected in parallel or in series.
The utility model discloses a gas-liquid separation device's backward flow volume is 0 with the ratio of top ejection of compact flow: 1-1000: 1, when the reflux ratio is 0, namely no reflux exists, the utility model can be used for producing distilled water with low energy consumption cost, and when the reflux ratio is not equal to 0, the utility model can be used for producing deuterium-depleted water with low energy consumption cost; the ratio of the top discharge flow to the feed flow is 0.01:1-1: 1.
the utility model discloses a gas-liquid separation device is rectifying column 3, and first heating device is vapor compression pump 4, and second heating device is reboiler 1, and the heat exchange tube 5 of heat transfer spare for being the W type.
A preparation method of deuterium-depleted water comprises the following steps:
feeding preheated or not preheated feed into a gas-liquid separation device for rectification operation, feeding a gas-phase material flowing out of one end (top) of the gas-liquid separation device into a first heating device, heating and pressurizing the gas-phase material, and feeding the gas-phase material into a heat exchange piece arranged in a second heating device;
one path of the material flowing out of the bottom of the gas-liquid separation device is extracted from the bottom of the gas-liquid separation device in a bottom discharging mode, the material can be selectively heated and then flows back to the gas-liquid separation device, the material can also be directly extracted without being heated, the other path of the material flowing out of the bottom of the gas-liquid separation device enters the second heating device and is not contacted with the material in the heat exchange piece, the material in the heat exchange piece is used as a heat source, the material from the gas-liquid separation device and positioned outside the heat exchange piece and the material in the heat exchange piece exchange heat in the second heating device, the material in the heat exchange piece is cooled and flows back to the top of the gas-liquid separation device, the material outside the heat exchange piece is heated and flows back to the bottom of the gas-liquid separation device, and required low deuterium water is generated at the top of the gas-liquid separation device; the material in the heat exchange piece is cooled and selectively flows back to the bent heat exchange tube 8 arranged in the third heating device and then exchanges heat with the feeding material entering the third heating device (located outside the bent heat exchange tube 8), one path of the material in the bent heat exchange tube 8 is extracted from the top of the third heating device in a top discharging mode, the other path of the material flows back to the top of the gas-liquid separation device, the material in the third heating device and located outside the bent heat exchange tube 8 enters the inside of the gas-liquid separation device, and the circulation is repeated in this way, so that high-yield low-deuterium water is realized.
The utility model also discloses an application of deuterium depleted water or distilled water that deuterium depleted water preparation method preparation obtained in the material that prepares deuterium depleted hydrogen water, deuterium depleted bubble water, deuterium depleted normal saline and contain deuterium depleted water or distilled water.
Example 1
As shown in fig. 2-4, a deuterium depleted water preparation device comprises a gas-liquid separation device, a first heating device, a second heating device and a third heating device, wherein the gas-liquid separation device is a rectifying tower 3, the first heating device is a steam compression pump 4, the second heating device is a reboiler 1, a heat exchange part arranged in the reboiler 1 is a W-shaped heat exchange tube 5, the third heating device is a heat exchanger 6, a bent heat exchange tube 8 arranged in the third heating device is W-shaped, the top of the rectifying tower 3 is communicated with the steam compression pump 4 and then communicated to the top of the heat exchange tube 5 arranged in the reboiler 1, the bottom of the heat exchange tube 5 is communicated with the top of the rectifying tower 3 through the bent heat exchange tube 8 and is used for enabling materials in the heat exchange tube 5 to flow back into the rectifying tower 3 through the top of the rectifying tower 3, and a part of the materials in the heat exchange tube 5 enters the bent heat exchange tube 8 and is extracted from the top of the heat exchanger 6 in a top discharging manner, as a finished product of deuterium-depleted water, the rest part of deuterium-depleted water flows back to the top of a rectifying tower 3, the bottom of the rectifying tower 3 is communicated with the inside of a reboiler 1 and cannot be communicated with a heat exchange tube 5, materials in the reboiler 1 and outside the heat exchange tube 5 can flow back to the bottom of the rectifying tower 3, the temperature of the materials in the heat exchange tube 5 is higher than that of the materials in the reboiler 1 and outside the heat exchange tube 5, after the materials in the reboiler 1 and outside the heat exchange tube 5 exchange heat with the materials in the heat exchange tube 5, the materials in the heat exchange tube 5 are cooled and flow back to the rectifying tower 3, the materials in the reboiler 1 and outside the heat exchange tube 5 are heated and flow back to the rectifying tower 3, it should be noted that a part of the materials at the bottom of the rectifying tower 3 can be directly extracted from the bottom of the rectifying tower 3 in a bottom discharging manner, and the rest of the materials are conveyed to the reboiler 1 for heat exchange and backflow.
In the reboiler 1, in the process of heating the material from the bottom of the rectifying tower 3, high-temperature and high-pressure steam in the heat exchange tube 5 can be cooled to be liquid water, one part of the material is taken as top discharge and is extracted, namely, the finished deuterium depleted water is obtained, and the other part of the material can be refluxed and then enters the rectifying tower 3 again to be circularly and repeatedly compressed, subjected to heat exchange and refluxed, so that the yield of the deuterium depleted water is improved.
For realizing preheating of feeding, the utility model discloses set up heat exchanger 6 rather than the intercommunication in 3 upper reaches of rectifying column, heat exchanger 6 can set up a plurality of, this embodiment 1 adopt a heat exchanger 6 can, feed (natural water, running water etc.) get into and preheat in the heat exchanger 6, the material in feed and the crooked heat exchange tube 8 separates through crooked heat exchange tube 8, can carry out the heat exchange, the feeding after preheating is carried to rectifying column 3 in, reduce the difference in temperature with the interior material of rectifying column 3, reduce subsequent heating energy consumption.
The feed is preheated by the heat exchanger 6 and then enters the rectifying tower 3, the steam flowing out of the top of the rectifying tower 3 directly enters the steam compression pump 4 and forms steam with higher temperature and higher pressure in the steam compression pump 4 through the compression and other prior art, the temperature and pressure of the steam are higher than the temperature and pressure of the materials in the rectifying tower 3 and are also higher than the temperature and pressure of the materials flowing out of the top and the bottom of the rectifying tower 3, the steam flowing out of the top of the rectifying tower 3 does not need to be condensed or cooled like the prior art, the energy consumption is reduced, the steam with higher temperature and higher pressure flowing out of the steam compression pump 4 enters the heat exchange tube 5 of the reboiler 1 and then is used as a heat source for heating subsequent materials and is used for carrying out heat exchange with the materials in the reboiler 1 and outside the heat exchange tube 5, the steam in the heat exchange tube 5 is cooled into liquid phase materials and then flows into the bent heat exchange tube 8, one part is directly extracted from the bent heat exchange tube 8 in a material ejection mode, and the other part flows back to the top of the rectifying tower 3; a part of liquid-phase materials at the bottom of the rectifying tower 3 can be directly extracted from a bottom kettle of the rectifying tower 3 in a bottom discharging mode, the bottom discharging mode can be a liquid mode or a gas mode, the bottom discharging temperature is 30-200 ℃, preferably 50-125 ℃, after the rest liquid-phase materials are conveyed to a reboiler 1, the liquid-phase materials are heated into gas phase (water vapor) by taking the high-temperature high-pressure steam compressed by the steam compression pump 4 as a heat source, and then the gas phase (water vapor) flows back to the bottom of the rectifying tower 3 to finish the rectifying process; the water vapor at the bottom of the rectifying tower 3, the liquid phase material refluxed at the top of the rectifying tower 3 and the feeding material are subjected to isotope exchange and separation processes, so that low-deuterium water is generated at the top of the rectifying tower 3, and water with deuterium content higher than that of natural concentration is generated at the bottom of the rectifying tower 3.
It should be noted that, the material of the liquid phase of rectifying column 3 bottom can adopt current heat exchanger equipment such as board-like, shell and tube to carry out further heat treatment with the form of end ejection of compact from rectifying column 3 bottom cauldron after extracting according to actual demand selectivity, and the later stage of being convenient for utilizes its waste heat, also can directly extract and need not to heat, and the heating step here is not the utility model discloses a necessary step also can be with the material conversion of the liquid phase of rectifying column 3 bottom to extract again behind liquid phase or the gaseous phase form.
For improving material transport efficiency, the utility model discloses can set up a plurality of delivery pumps 7 according to the suitable position of actual demand between reboiler 1 and rectifying column 3, material in the heat exchange tube 5 flows back to the in-process in rectifying column 3 can use delivery pump 7 to transport, and the material of the liquid phase of rectifying column 3 bottom is adopted or is carried to reboiler 1's in-process also can use delivery pump 7 to transport, can also carry out the material through other current modes such as siphon effect or high head and carry out the material transport.
The material entering the rectifying tower 3 can be in a liquid form, a gas form or a gas-liquid mixed form, the temperature of the material entering the rectifying tower 3 is 0-150 ℃, preferably 50-100 ℃, the feeding amount is 0.001Kg/h-1000000Kg/h, preferably 10-1000Kg/h, the feeding amount is not limited, and the feeding amount can be flexibly set according to actual requirements.
The vapor flowing out of the top of the rectifying column 3 has a temperature of 20 to 200 c, preferably 40 to 120 c, a temperature of 30 to 300 c, preferably 65 to 140 c, as a vapor formed after passing through the vapor compression pump 4, and a pressure of 5 to 500KPa (absolute), preferably 25 to 300KPa (absolute).
The deuterium content in the bottom discharge of the rectifying tower 3 accounts for 0.015-100% of the total amount of the bottom discharge; preferably 0.1 to 10%.
The ratio of the reflux amount of the rectifying tower 3 to the top discharge flow, namely the reflux ratio, is 0: 1-1000: 1, preferably 10: 1-100: 1, if the reflux ratio is 0, distilled water, cool boiled water and the like with high purity and meeting the drinking water standard can be synchronously produced, and the main difference of the method and the existing products is that the deuterium content is not obviously reduced; the ratio of the top discharge flow to the feed flow is from 0.01:1 to 1:1, and the deuterium content in the top discharge is from 0.01 to 150ppm, preferably from 25 to 100 ppm. The rectifying tower 3 may have a single tower structure, or a plurality of towers may be connected in parallel or in series. The material extracted from the bottom of the rectifying tower 3 can be used for preheating the feeding material through a heat exchanger, so that the heat energy of the material can be utilized.
Example 2
As shown in fig. 2-3 and 5, a deuterium depleted water preparation apparatus includes a gas-liquid separation device, a first heating device, a second heating device and a third heating device, and the difference between this embodiment 2 and embodiment 1 is that two third heating devices arranged in parallel and sequentially connected end to end are arranged at the upstream of the gas-liquid separation device, and in this embodiment 2, a feed enters another heat exchanger 6 after being heat-exchanged by a heat exchanger 6 farthest from a rectifying tower 3, and then enters the rectifying tower 3, and a material flowing out from the bottom of the gas-liquid separation device is preheated by a third heating device closest to the gas-liquid separation device after being extracted from the bottom of the rectifying tower 3 or from the bottom in the form of bottom discharge.
The gas-liquid separation device is a rectifying tower 3, the first heating device is a steam compression pump 4, the second heating device is a reboiler 1, a heat exchange piece arranged in the reboiler 1 is a W-shaped heat exchange tube 5, the third heating device is a heat exchanger 6, and a bent heat exchange tube 8 arranged in the third heating device is W-shaped.
The top of a rectifying tower 3 is communicated with a vapor compression pump 4 and then communicated to the top of a heat exchange tube 5 arranged in a reboiler 1, the bottom of the heat exchange tube 5 is communicated with the bottom of a bent heat exchange tube 8 in a heat exchanger 6 farthest from the rectifying tower 3, the top of the bent heat exchange tube 8 is communicated with the top of the rectifying tower 3 and is used for enabling materials in the heat exchange tube 5 to flow back into the rectifying tower 3 through the top of the rectifying tower 3, the bottom of the rectifying tower 3 is communicated with the interior of the reboiler 1 and cannot be communicated with the heat exchange tube 5, materials in the reboiler 1 and outside the heat exchange tube 5 can flow back to the bottom of the rectifying tower 3 after heat exchange, the temperature of the materials in the heat exchange tube 5 is higher than that of the materials in the reboiler 1 and outside the heat exchange tube 5, the materials in the reboiler 1 and outside the heat exchange tube 5 are cooled, and a part of the materials in the heat exchange tube 5 flows back into the rectifying tower 3, and the other part is directly extracted in a top discharging mode, and materials in the reboiler 1 and positioned outside the heat exchange tube 5 are heated and flow back to the bottom of the rectifying tower 3. It should be noted that a part of the material at the bottom of the rectifying tower 3 can be directly extracted from the bottom of the rectifying tower 3 in a bottom discharging manner, and then the part of the material can be sent to the bent heat exchange tube 8 arranged in the heat exchanger 6 closest to the gas-liquid separation device for preheating treatment and then discharged, the part of the material can be directly extracted without preheating, and the rest material at the bottom of the rectifying tower 3 is sent to the reboiler 1.
The same as in example 1.
Example 3
As shown in fig. 2-3 and fig. 6, the present embodiment 3 is different from the embodiment 2 in that two heat exchangers 6 of the present embodiment 3 need not be arranged in parallel, but only need to ensure communication, the top of the rectifying tower 3 is communicated with a vapor compression pump 4 and then communicated to the top of a heat exchange tube 5 arranged in a reboiler 1, the bottom of the heat exchange tube 5 is communicated with one end of a curved heat exchange tube 8 arranged in one of the heat exchangers 6, the other end of the curved heat exchange tube 8 can directly extract part of the deuterium depleted water from the inside of the curved heat exchange tube 8, the rest of the material in the curved heat exchange tube 8 flows back to the rectifying tower 3 from the top of the rectifying tower 3, the material in the heat exchanger 6 and outside the curved heat exchange tube 8 can directly enter the rectifying tower 3, the other heat exchanger 6 is used as an initial feeding end and can preheat the material discharged from the bottom of the rectifying tower 3 and then discharge the material, at the moment, a part of the material at the bottom of the rectifying tower 3 can be directly extracted from the bottom of the rectifying tower 3 in a bottom discharging mode, then enters a bent heat exchange tube 8 arranged in the heat exchanger 6, exchanges heat with the material outside the bent heat exchange tube 8 and then is discharged out of the heat exchanger 6, and the remaining liquid phase material at the bottom of the rectifying tower 3 is conveyed to the reboiler 1.
Example 4
The feeding temperature entering the rectifying tower 3 is 100 ℃, the water vapor temperature at the top of the rectifying tower 3 is 100 ℃, the water vapor temperature formed after the water vapor at the top of the rectifying tower 3 enters the vapor compression pump 4 for compression is 121 ℃, and the pressure is 100KPa (gauge pressure);
in the operation process, the feeding flow of the rectifying tower 3 is 100Kg/h, the top discharge of the rectifying tower 3 is 80ppm, the top discharge flow is 58.8Kg/h, the reflux is 58800Kg/h, and the reflux ratio is 1000: 1.
the temperature of the bottom of the rectifying tower 3 is 105 ℃, the discharge flow of the bottom of the rectifying tower 3 is 41.2Kg/h, and the deuterium content in the discharge of the bottom is 250 ppm.
Example 5
The feeding temperature of the steam entering the rectifying tower 3 is 50 ℃, the temperature of the steam at the top of the rectifying tower 3 is 120 ℃, the temperature of the steam formed after the steam at the top of the rectifying tower 3 enters the steam compression pump 4 for compression is 140 ℃, and the pressure is 300KPa (gauge pressure);
in the operation process, the feeding flow of the rectifying tower 3 is 1000Kg/h, the top discharge of the rectifying tower 3 is 110ppm, the top discharge flow is 789.5Kg/h, the reflux is 15790Kg/h, and the reflux ratio is 20: 1; the temperature of the bottom of the rectifying tower 3 is 125 ℃, the flow rate of bottom discharge is 210.5Kg/h, and the deuterium content in the bottom discharge is 300 ppm.
Example 6
The feeding temperature of the feed entering the rectifying tower 3 is 20 ℃, the temperature of the steam at the top of the rectifying tower is 40 ℃, the temperature of the steam formed after the steam at the top of the rectifying tower 3 enters the steam compression pump 4 for compression is 65 ℃, and the pressure is 25KPa (absolute pressure);
in the operation process, the feeding flow of the rectifying tower 3 is 10 Kg/h; the discharge at the top of the rectifying tower 3 is 50ppm, and the discharge flow at the top of the rectifying tower is 6 Kg/h; the reflux amount is 60Kg/h, and the reflux ratio is 10: 1; the temperature at the bottom of the tower is 50 ℃, the flow rate of bottom discharge is 4Kg/h, and the deuterium content in the bottom discharge is 300 ppm.
Example 7
The feeding temperature of the feed entering the rectifying tower 3 is 60 ℃, the temperature of the steam at the top of the rectifying tower is 75 ℃, the temperature of the steam formed after the steam at the top of the rectifying tower 3 enters the steam compression pump 4 for compression is 92 ℃, and the pressure is 75KPa (absolute pressure);
in the operation process, the feeding flow of the rectifying tower 3 is 100 Kg/h; the discharge at the top of the tower is 30ppm, and the discharge flow at the top of the tower is 80 Kg/h; the reflux amount is 2400Kg/h, and the reflux ratio is 30: 1; the temperature of the bottom of the column was 82 ℃, the flow rate of the bottom discharge was 20Kg/h, and the deuterium content in the bottom discharge was 650 ppm.
The utility model has the advantages that:
1. the existing low-temperature rectification technology needs to cool materials at the top or the top of a rectifying tower 3, generally uses cooling circulating water to cool through a condenser 2, and the utility model saves the cooling link of the condenser 2 and directly compresses steam;
2. the existing rectification technology needs to be separately externally connected with a heating source, such as industrial steam, and can consume more energy consumption, the heating source of the utility model is the steam which flows out from the top of the rectification tower 3 and is compressed by the steam compression pump 4, and only a small amount of energy consumption needs to be provided because no phase change exists, the energy consumption is greatly reduced, and the energy recycling is realized;
3. the top discharge and the bottom discharge exchange heat through feeding, so that the materials are preheated, the temperature difference is reduced, and the heating energy consumption is reduced; the top and bottom materials are cooled in the heat exchange process, so that the energy consumption required by cooling is reduced;
4. high-quality drinking water such as distilled water or cool boiled water can be prepared only by setting the reflux ratio of the rectifying tower 3 to 0, the deuterium content of the drinking water is slightly lower than that of deuterium-depleted water, the multifunctional water-saving distillation tower has multiple purposes, and is strong in practicability and wide in application range.
The utility model discloses the part of not specifically describing adopt prior art can, do not describe here any more.
The above only is the embodiment of the present invention, not limiting the patent scope of the present invention, all the equivalent structures or equivalent processes that are used in the specification and the attached drawings or directly or indirectly applied to other related technical fields are included in the patent protection scope of the present invention.
Claims (8)
1. The utility model provides a deuterium-depleted water preparation facilities, its characterized in that, includes gas-liquid separation device, first heating device and second heating device, gas-liquid separation device one end communicates to the built-in heat transfer spare one end of second heating device through first heating device, and the heat transfer spare other end communicates gas-liquid separation device, and the gas-liquid separation device other end communicates with the inside intercommunication of second heating device and not communicate with the heat transfer spare, and the temperature of the material in the heat transfer spare is greater than the temperature of the material that gas-liquid separation device top and bottom flowed out, and the material that comes from gas-liquid separation device and be located the heat transfer spare outside carries out the heat exchange with the material in the heat transfer spare in the second heating device.
2. The deuterium depleted water preparation device of claim 1, wherein the top of the gas-liquid separation device is connected to one end of the heat exchange member through a first heating device, the opposite end of the heat exchange member is connected to the top of the gas-liquid separation device, and the bottom of the gas-liquid separation device is connected to the inside of a second heating device and is not connected to the heat exchange member.
3. The deuterium-depleted water preparation device of claim 1, further comprising a plurality of communicated third heating devices, wherein the third heating devices are internally provided with bent heat exchange tubes, one end of the heat exchange member is communicated to the top of the gas-liquid separation device through the first heating device, the other end of the heat exchange member is selectively communicated with the top of the gas-liquid separation device through the bent heat exchange tubes in zero or one of the third heating devices, one path of the bottom of the gas-liquid separation device is communicated with the inside of the second heating device and is not communicated with the heat exchange member, the other path of the bottom of the gas-liquid separation device is selectively communicated with the bent heat exchange tubes in zero or one of the third heating devices, and a feed material in the third heating device and outside the bent heat exchange tubes is subjected to heat exchange with a material in the bent heat exchange tubes and then enters the gas-liquid separation device.
4. The deuterium depleted water preparation device of claim 3, wherein the third heating device is a heat exchanger, and the bent heat exchange tube arranged inside the third heating device is W-shaped.
5. The deuterium depleted water preparation device of claim 1, wherein a material transfer device is disposed between the gas-liquid separation device and the second heating device, and the material transfer device is a transfer pump.
6. The deuterium depleted water production apparatus of claim 1, wherein a ratio of a reflux volume to an overhead discharge volume of the gas-liquid separation device is 0: 1-1000: 1, the ratio of the top discharge flow to the feed flow is 0.01:1-1:1, the deuterium content in the top discharge is 0.01-150 ppm.
7. The deuterium depleted water production apparatus of claim 1, wherein there are several gas-liquid separation devices, and the several gas-liquid separation devices are connected in parallel or in series.
8. The deuterium depleted water production apparatus of claim 1, wherein the gas-liquid separation device is a rectifying column, the first heating device is a vapor compression pump, the second heating device is a reboiler, and the heat exchange member is W-shaped.
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| CN202023295034.8U CN214158564U (en) | 2020-12-30 | 2020-12-30 | Deuterium-depleted water preparation device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202023295034.8U CN214158564U (en) | 2020-12-30 | 2020-12-30 | Deuterium-depleted water preparation device |
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| CN214158564U true CN214158564U (en) | 2021-09-10 |
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