Device and method for multistage continuous preparation of deuterium depleted water

Abstract

The present application discloses a method for preparing deuterium depleted water, wherein natural water is fed into the device of the present disclosure, and the liquid phase stream continuously flows backwards stage by stage under the combined action of the low-pressure steam compressors and the stream delivery pumps. In a single-stage system, the deuterium is deprived depending on the difference in vapor pressure between .sup.1H.sub.2O and .sup.2H.sub.2O (and/or .sup.1H.sup.2HO), and finally, the deuterium depleted water is produced.

Claims

1. A process for preparing deuterium depleted water by a device for multistage continuous preparation of deuterium depleted water; wherein the device for multistage continuous preparation of deuterium depleted water comprises a feeding pump, a plurality of stages of separation systems connected in series, and a receiver, wherein each stage of separation systems comprises a distillation column, a vapor-liquid separator, a low-pressure steam compressor, a stream delivery pump, a three-way valve, and a stream output pipe; wherein: the distillation column comprises a plurality of column sections arranged vertically from top to bottom, and a liquid phase vaporizer located at the bottom of the column; the distillation column is provided with a first liquid phase return inlet, a second liquid phase return inlet and a steam outlet at the top of the column, a liquid phase inlet at the middle of the column, and a waste liquid outlet at the bottom of the column; the liquid phase vaporizer is provided with a steam inlet in an upper part thereof and a stream outlet in a lower part thereof, the steam inlet and the stream outlet are connected through a hollow tube; the stream delivery pump has a stream inlet and a stream outlet; the three-way valve has three ports; the vapor-liquid separator is provided with a vapor phase inlet in the middle thereof, a vapor phase outlet in the top thereof, and a liquid phase outlet in the bottom thereof; the steam outlet of the distillation column is connected to the vapor phase inlet of the vapor-liquid separator, while the vapor phase outlet of the vapor-liquid separator is connected to an inlet of the low-pressure steam compressor and an outlet of the low-pressure steam compressor is connected to the steam inlet of the liquid phase vaporizer; the liquid phase outlet of the vapor-liquid separator is connected to the first liquid phase return inlet of the distillation column; the stream outlet of the liquid phase vaporizer of the distillation column is connected to the stream inlet of the stream delivery pump, and the three ports of the three-way valve are respectively connected to the stream outlet of the stream delivery pump, the second liquid phase return inlet of the distillation column and the stream output pipe; the feeding pump is connected ahead of the liquid phase inlet of the distillation column in a first-stage separation system; the stream output pipe of a last-stage separation system is connected to the receiver, and the stream output pipe of each of the other stages of separation systems is connected to the liquid phase inlet of the distillation column in a next-stage separation system; and all the connections are achieved by means of pipes; the process comprising: (1) feeding a natural water as a liquid phase feed into the device for multistage continuous preparation of deuterium depleted water by the feeding pump; wherein the distillation column has the following parameters: a column top operating pressure of 50-760 mmHg, a column top temperature of 38-110° C., a column bottom operating pressure of 200-900 mmHg, and a column bottom temperature 67-110° C.; (2) delivering the liquid phase feed into the distillation column through the liquid phase inlet and vaporizing the liquid phase feed under the action of the liquid phase vaporizer thereby obtaining a vapor phase stream that ascends in the distillation column and entering the vapor-liquid separator through the steam outlet for vapor-liquid separation, in each stage of separation systems; returning a liquid phase obtained in the vapor-liquid separator to the distillation column through the liquid phase outlet and the first liquid phase stream return inlet in sequence to be part of the liquid phase stream; discharging a vapor phase obtained in the vapor-liquid separator through the vapor phase outlet to the low-pressure steam compressor and then compressing the vapor phase to a high temperature and high pressure steam; the high temperature and high pressure steam-entering the hollow tube through the steam inlet and exchanging heat with the liquid phase stream in the liquid phase vaporizer; draining the liquid phase stream obtained after heat release and condensation out of the stream outlet into the stream delivery pump, and returning a part of the liquid phase stream to the distillation column through the second liquid phase stream return inlet by means of the three-way valve for continuous distillation, while discharging the other part of the liquid phase stream to a next-stage separation system or into the receiver through the stream output pipe; and (3) receiving a deuterium depleted water continuously or intermittently in the receiver.

2. The process of claim 1, further comprising: (4) draining part of the liquid phase stream in the liquid phase vaporizer out of the device as waste liquid through the waste liquid outlet at the bottom of any of the distillation column during step (2) in each stage of separation systems.

3. The process of claim 1, wherein the number of the separation systems is 1˜10.

4. The process of claim 1, wherein the number of the column sections is 1˜30.

5. The process of claim 4, wherein the column section is composed of a liquid phase collecting distributor, a mass transfer stage element, and a vapor phase distributor.

6. The process of claim 5, wherein the mass transfer stage element is a random mass transfer stage element or a structured mass transfer stage element.

7. The process of claim 6, wherein the random mass transfer stage element is a Dixon random mass transfer stage element of which a height equivalent to a theoretical plate is 1 cm to 4 cm, and the structured mass transfer stage element is a corrugated mass transfer stage element of which a height equivalent to a theoretical plate is 2 cm to 6 cm.

8. The process of claim 7, wherein the material of the mass transfer stage element is hydrophilic material.

9. The process of claim 8, wherein the hydrophilic material is a phosphorous bronze material.

10. The process of claim 1, wherein an electric heater is further arranged in the liquid phase vaporizer.

11. The process of claim 1, wherein the liquid phase inlet is located between the last column section and the liquid phase vaporizer.

Description

BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS

(1) FIG. 1 is a process flow diagram of a device and method for multistage continuous preparation of deuterium depleted water according to the present invention, wherein the arrows indicate stream flow directions, and wherein the device comprises a feeding pump S, a receiving device P, and n stages of separation systems; the first-stage separation system comprising a distillation column 1A, a vapor-liquid separator 1B, a low-pressure steam compressor 1C, a stream delivery pump 1D, a three-way valve 1E, and a stream output pipe 1F; the n-stage separation system comprising a distillation column nA, a vapor-liquid separator nB, a low-pressure steam compressor nC, a stream delivery pump nD, a three-way valve nE, and a stream output pipe nF, n being a positive integer.

(2) FIG. 2 is a schematic diagram of a single-stage distillation column according to the present invention, wherein the single-stage distillation column comprises a distillation column nA, a vapor-liquid separator nB, a low-pressure steam compressor nC, a stream delivery pump nD, a three-way valve nE, and a stream output pipe nF, n being a positive integer.

(3) FIG. 3 is a process flow diagram of a two-stage device of embodiment 1 and 4.

(4) FIG. 4 is a process flow diagram of a three-stage device of embodiment 2.

(5) FIG. 5 is a process flow diagram of a six-stage device of embodiment 3.

DETAILED DESCRIPTION OF THE INVENTION

(6) The present invention can be better understood according to the following examples. However, it would be easy for a person skilled in the art to understand that the contents described in the examples are merely intended to illustrate the present invention rather than limit the present invention described in detail in the claims.

Embodiment 1

(7) Natural water containing the deuterium isotope with an abundance of 150 ppm as feed is fed into the device of the present invention. A two-stage system is connected in series. A separation column section of a distillation column in a first-stage system is provided with a corrugated structured mass transfer stage element of which the height equivalent to a theoretical plate (HETP) is 6.0 cm, and a low-pressure steam compressor, which is a 20 KW power compressor, is adjustable within a frequency range of 40 to 50 Hz. An operating pressure at the top of the first-stage distillation column is controlled to 760 mmHg (absolute pressure) and an operating temperature is controlled to 100° C. A separation column section of a distillation column in a second-stage system is provided with a corrugated structured mass transfer stage element of which the height equivalent to a theoretical plate (HETP) is 4.0 cm, and a low-pressure steam compressor, which is a 10 KW power compressor, is adjustable within a frequency range of 40 to 50 Hz. An operating pressure at the top of the second-stage distillation column is controlled to 500 mmHg (absolute pressure) and an operating temperature is controlled to 88° C.

(8) The natural water feed, i.e., a liquid phase stream, is fed into a liquid phase inlet 1A05 in the middle of the first-stage distillation column 1A by a feeding pump S and flows to a liquid phase vaporizer 1A03 at the bottom, and then is heated to vaporize. Specifically, the liquid phase stream is heated to vaporize by an electric heater 1A13 arranged in the liquid phase vaporizer 1A03 in an initial heating period, and in a normal start-up period, heated to vaporize by a high-temperature and high-pressure vapor phase stream, i.e., steam, that is formed by compressing the vapor phase stream in the top using a low-pressure steam compressor 1B. The vapor phase stream ascends in the distillation column 1A and enters a vapor-liquid separator 1B through a steam outlet 1A06 for vapor-liquid separation.

(9) The liquid phase obtained in the vapor-liquid separator 1B returns to the distillation column 1A through a liquid phase outlet 1B03 and a first liquid phase stream return inlet 1A08 in sequence to be part of the liquid phase stream. The vapor phase obtained in the vapor-liquid separator 1B enters and is compressed by a low-pressure steam compressor 1C into high-temperature and high-pressure steam, and the steam enters a hollow tube 1A12 through a steam inlet 1A04 for heat exchange with the liquid phase stream in the liquid phase vaporizer 1A03. The liquid phase stream obtained after heat release and condensation is drained out of a stream outlet 1A02 into a stream delivery pump 1D, and part of the liquid phase stream is returned to the distillation column 1A through a second liquid phase stream return inlet 1A07 by means of a three-way valve 1E for continuous distillation, while the other part of the liquid phase stream is discharged to a liquid phase inlet 2A05 of the second-stage separation system through a stream output pipe 1F and flows to a liquid phase vaporizer 2A03 at the bottom, and then is heated to vaporize. The vapor phase stream ascends in a distillation column 2A and enters a vapor-liquid separator 2B through a steam outlet 2A06 for vapor-liquid separation.

(10) The liquid phase obtained in the vapor-liquid separator 2B returns to the distillation column 2A through a liquid phase outlet 2B03 and a first liquid phase stream return inlet 2A08 in sequence to be part of the liquid phase stream. The vapor phase obtained in the vapor-liquid separator 2B enters and is compressed by a low-pressure steam compressor 2C into high-temperature and high-pressure steam, and the steam enters a hollow tube 2A12 through a steam inlet 2A04 for heat exchange with the liquid phase stream in the liquid phase vaporizer 2A03. The liquid phase stream obtained after heat release and condensation is drained out of a stream outlet 2A02 into a stream delivery pump 2D, and part of the liquid phase stream is returned to the distillation column 2A through a second liquid phase stream return inlet 2A07 by means of a three-way valve 2E for continuous distillation, while the other part of the liquid phase stream is discharged to a receiver P through a stream output pipe 2F, thereby obtaining the deuterium depleted water product with a deuterium content of 100 ppm.

(11) Part of the liquid phase stream in the liquid phase vaporizer nA03 is drained out of the system as waste liquid.

(12) TABLE-US-00001 TABLE 1 Operating parameter table of the two-stage process device of embodiment 1 Operating parameter First Stage Second Stage Pump Feeding pump S: whirlpool pump 25NPD07Z; Stream delivery pump: whirlpool pump 20NPD07Z. Liquid phase feed flow Feed to 1A05 200 Feed to 2A05 175 Kg/h (150 ppm) Kg/h (120 ppm) Liquid phase return flow Liquid phase return Liquid phase return through 1A07 600 Kg/h through 2A07 250 Kg/h Condensed liquid phase Liquid phase output Liquid phase output flow through 1A02 775 Kg/h through 2A02 425 Kg/h Low-pressure steam flow Low-pressure steam flow Low-pressure steam flow into 1C 775 Kg/h into 2C 425 Kg/h Waste liquid flow Waste liquid through Waste liquid through 1A01 25 Kg/h (360 ppm) 2A01 5 Kg/h (800 ppm) Product flow From 2A05 to next-stage Product 170 Kg/h system 175 Kg/h (120 ppm) (100 ppm) Structural parameters of diameter 800 mm, height diameter 400 mm, height the distillation column 2500 mm, number of the 1500 mm, number of the column sections 10. column sections 15. Operating pressure at the 760 mmHg 500 mmHg top of the distillation column Operating temperature at 100° C. 88° C. the top of the distillation column Operating pressure at the 900 mmHg 650 mmHg bottom of the distillation column Operating temperature at 104° C. 96° C. the bottom of the distillation column Type of low pressure Roltz steam compressor Roltz steam compressor steam compressor ZQRSR-200 ZQRSR-100 Parameters Inlet 760 mmHg 500 mmHg of the pressure low-pressure Outlet 900 mmHg 650 mmHg steam pressure compressors Power 20 KW 10 KW Adjustable 40-50 Hz 40-50 Hz frequency Parameters Heat 1.36 m.sup.2 0.75 m.sup.2 of the liquid exchange phase area vaporizers Electric 40 KW 20 KW heating power Parameters of the Corrugated structured Corrugated structured distillation columns mass transfer stage element: mass transfer stage element: Height equivalent to a Height equivalent to a theoretical plate 6.0 cm theoretical plate 4.0 cm Assumed steam 775 Kg/h 425 Kg/h vaporized liquid phase flow in use Required heat energy 465 KW 255 KW supply Electric power used in 60 KW 30 KW the present process System heat loss 10% 46.5 KW 25.5 KW taken into consideration Energy saved 77.1% 78.2% Notes: the heat of vaporization of water is calculated by 2200 KJ/Kg (0.6 KWh/kg).

Embodiment 2

(13) Natural water containing the deuterium isotope with an abundance of 155 ppm as feed is fed into the device of the present invention. A three-stage system is connected in series to form a series stage. A separation column section of a distillation column in a first-stage system is provided with a corrugated structured mass transfer stage element of which the height equivalent to a theoretical plate (HETP) is 5.0 cm, and a low-pressure steam compressor, which is a 30 KW power compressor, is adjustable within a frequency range of 40 to 50 Hz. An operating pressure at the top of the first-stage distillation column is controlled to 760 mmHg (absolute pressure) and an operating temperature is controlled to 100° C. A separation column section of a distillation column in a second-stage system is provided with a corrugated structured mass transfer stage element of which the height equivalent to a theoretical plate (HETP) is 3.5 cm, and a low-pressure steam compressor, which is a 20 KW power compressor, is adjustable within a frequency range of 40 to 50 Hz. An operating pressure at the top of the second-stage distillation column is controlled to 500 mmHg (absolute pressure) and an operating temperature is controlled to 88° C. A separation column section of a distillation column in a third-stage system is provided with a corrugated structured mass transfer stage element of which the height equivalent to a theoretical plate (HETP) is 2.0 cm, and a low-pressure steam compressor, which is a 10 KW power compressor, is adjustable within a frequency range of 40 to 50 Hz. An operating pressure at the top of the second-stage distillation column is controlled to 240 mmHg (absolute pressure) and an operating temperature is controlled to 70° C.

(14) A vapor phase stream ascends in the distillation column 2A and enters a vapor-liquid separator 2B through a steam outlet 2A06 for vapor-liquid separation.

(15) The liquid phase obtained in the vapor-liquid separator 2B returns to the distillation column 2A through a liquid phase outlet 2B03 and a first liquid phase stream return inlet 2A08 in sequence to be part of the liquid phase stream. The vapor phase obtained in the vapor-liquid separator 2B enters and is compressed by a low-pressure steam compressor 2C into high-temperature and high-pressure steam, and the steam enters a hollow tube 2A12 through a steam inlet 2A04 for heat exchange with the liquid phase stream in the liquid phase vaporizer 1A03. The liquid phase stream obtained after heat release and condensation is drained out of a stream outlet 2A02 into a stream delivery pump 2D, and part of the liquid phase stream is returned to the distillation column 2A through a second liquid phase stream return inlet 2A07 by means of a three-way valve 2E for continuous distillation, while the other part of the liquid phase stream is discharged to a liquid phase inlet 3A05 of the third-stage separation system through a stream output pipe 2F and flows to a liquid phase vaporizer 3A03 at the bottom, and then is heated to vaporize. The vapor phase stream ascends in a distillation column 3A and enters a vapor-liquid separator 3B through a steam outlet 3A06 for vapor-liquid separation.

(16) The liquid phase obtained in the vapor-liquid separator 3B returns to the distillation column 3A through a liquid phase outlet 3B03 and a first liquid phase stream return inlet 3A08 in sequence to be part of the liquid phase stream. The vapor phase obtained in the vapor-liquid separator 3B enters and is compressed by a low-pressure steam compressor 3C into high-temperature and high-pressure steam, and the steam enters a hollow tube 3A12 through a steam inlet 3A04 for heat exchange with the liquid phase stream in the liquid phase vaporizer 3A03. The liquid phase stream obtained after heat release and condensation is drained out of a stream outlet 3A02 into a stream delivery pump 3D, and part of the liquid phase stream is returned to the distillation column 3A through a second liquid phase stream return inlet 3A07 by means of a three-way valve 3E for continuous distillation, while the other part of the liquid phase stream is discharged to a receiver P through a stream output pipe 3F, thereby obtaining the deuterium depleted water product with a deuterium content of 50 ppm.

(17) Part of the liquid phase stream in the liquid phase vaporizer nA03 is drained out of the system as waste liquid.

(18) TABLE-US-00002 TABLE 2 Operating parameter table of the three-stage process device of embodiment 2 Operating parameter First Stage Second Stage Third Stage Pump Feeding pump S: whirlpool pump 25NPD07Z; Stream deliver pump: whirlpool pump 25NPD07Z. Liquid phase feed flow Feed to 1A05 Feed to 2 A05 Feed to 3 A05 250 Kg/h (155 225 Kg/h (105.6 215 Kg/h (80.3 ppm) ppm) ppm) Liquid phase return flow Liquid phase Liquid phase Liquid phase return through return through return through 1A07 2A07 3A07 600 Kg/h 400 Kg/h 200 Kg/h Condensed liquid phase Liquid phase Liquid phase Liquid phase flow output through output through output through 1A02 2A02 3A02 825 Kg/h 615 Kg/h 405 Kg/h Low-pressure steam flow Low-pressure Low-pressure Low-pressure steam flow into steam flow into steam flow into 1C 825 Kg/h 2C 615 Kg/h 3C 405 Kg/h Waste liquid flow Waste liquid Waste liquid Waste liquid through 1A01 through 2A01 through 3A01 25 Kg/h (600 10 Kg/h (650 10 Kg/h (700 ppm) ppm) ppm) Product flow From 2A05 into From 3A05 into Product 205 next stage 225 next stage 215 Kg/h (50 ppm) Kg/h (105.6 ppm) Kg/h (80.3 ppm) Structural parameters of diameter 800 mm, diameter 600 mm, diameter 400 mm, the distillation column height 2500 mm, height 2500 mm, height 1500 mm, number of the number of the number of the column sections column sections column sections 10. 10. 15. Operating pressure at the 760 mmHg 500 mmHg 240 mmHg top of the distillation column Operating temperature at 100° C. 88° C. 70° C. the top of the distillation column Operating pressure at the 900 mmHg 650 mmHg 400 mmHg bottom of the distillation column Operating temperature at 104° C. 96° C. 83° C. the bottom of the distillation column Type of low pressure Roltz steam Roltz steam Roltz steam steam compressor compressor compressor compressor ZQRSR-300 ZQRSR-200 ZQRSR-100 Parameters Inlet 760 mmHg 500 mmHg 240 mmHg of the pressure low-pressure Outlet 900 mmHg 650 mmHg 400 mmHg steam pressure compressors Power 30 KW 20 KW 10 KW Adjustable 40-50 Hz 40-50 Hz 40-50 Hz frequency Parameters Heat 1.49 m.sup.2 1.09 m.sup.2 0.71 m.sup.2 of the liquid exchange phase area vaporizers Electric 50 KW 40 KW 30 KW heating power Parameters of the Corrugated Corrugated Corrugated distillation columns structured mass structured mass structured mass transfer stage transfer stage transfer stage element: element: element: Height Height Height equivalent to equivalent to equivalent to a theoretical a theoretical a theoretical plate 5.0 cm plate 3.5 cm plate 2.0 cm Assumed steam 825 Kg/h 615 Kg/h 505 Kg/h vaporized liquid phase flow in use Required heat energy 495 KW 369 KW 303 KW supply Electric power used in 80 KW 60 KW 40 KW the present process System heat loss 10% 49.5 KW 36.9 KW 30.3 KW taken into consideration Energy saved 73.8% 73.7% 76.8% Notes: the heat of vaporization of water is calculated by 2200 KJ/Kg (0.6 KWh/Kg).

Embodiment 3

(19) Natural water containing the deuterium isotope with an abundance of 145 ppm as feed is fed into the device of the present invention. A six-stage system is connected in series to form a series stage.

(20) The system and operation parameters are shown in table 3.

(21) The natural water feed, i.e., a liquid phase stream, is fed into a liquid phase inlet 1A05 in the middle of the first-stage distillation column 1A by a feeding pump S and flows to a liquid phase vaporizer 1A03 at the bottom, and then is heated to vaporize. Specifically, the liquid phase stream is heated to vaporize by an electric heater 1A13 arranged in the liquid phase vaporizer 1A03 in an initial heating period, and in a normal start-up period, heated to vaporize by a high-temperature and high-pressure vapor phase stream, i.e., steam, that is formed by compressing the vapor phase stream in the top using a low-pressure steam compressor 1B. The vapor phase stream ascends in the distillation column 1A and enters a vapor-liquid separator 1B through a steam outlet 1A06 for vapor-liquid separation.

(22) The liquid phase obtained in the vapor-liquid separator 1B returns to the distillation column 1A through a liquid phase outlet 1B03 and a first liquid phase stream return inlet 1A08 in sequence to be part of the liquid phase stream. The vapor phase obtained in the vapor-liquid separator 1B enters and is compressed by a low-pressure steam compressor 1C into high-temperature and high-pressure steam, and the steam enters a hollow tube 1A12 through a steam inlet 1A04 for heat exchange with the liquid phase stream in the liquid phase vaporizer 1A03. The liquid phase stream obtained after heat release and condensation is drained out of a stream outlet 1A02 into a stream delivery pump 1D, and part of the liquid phase stream is returned to the distillation column 1A through a second liquid phase stream return inlet 1A07 by means of a three-way valve 1E for continuous distillation, while the other part of the liquid phase stream is discharged to a liquid phase inlet 2A05 of the second-stage separation system through a stream output pipe 1F.

(23) Following the same path and in the same manner, the liquid phase stream continuously passes through the second stage, the third stage, the four stage, the fifth stage and the fifth stage that are connected in series. After six times of deprivation of the deuterium, part of the liquid phase stream from the vapor phase stream after heat release and condensation is delivered to a liquid phase return inlet 6A07 in the top of the sixth stage, while the rest is discharged to a receiver P through a stream output pipe 6F, thereby obtaining the deuterium depleted water product with a deuterium content of 1 ppm.

(24) Part of the liquid phase stream in the liquid phase vaporizer nA03 is drained out of the system as waste liquid.

(25) TABLE-US-00003 TABLE 3 Operating parameter table of the six-stage process device of embodiment 3 Operating Second Third Fourth Fifth Sixth Parameter First Stage Stage Stage Stage Stage Stage Pump Feeding pump S, Stream delivery pump 2D and 3D: whirlpool pump 25NPD07Z; Stream delivery pump 4D~6D: whirlpool pump 20NPD07Z Liquid phase Feed to Feed to Feed to Feed to Feed to Feed to feed flow 1A05 2A05 3A05 4A05 5A05 6A05 250 Kg/h 225 Kg/h 200 Kg/h 175 Kg/h 150 Kg/h 140 Kg/h (145 ppm) (133.3 (117.5 (95.7 (65 ppm) (41.1 ppm) ppm) ppm) ppm) Liquid phase Liquid Liquid Liquid Liquid Liquid Liquid return flow phase phase phase phase phase phase return return return return return return through through through through through through 1A07 2A07 3A07 4A07 300 5A07 6A07 600 Kg/h 400 Kg/h 400 Kg/h Kg/h 200 Kg/h 200 Kg/h Condensed Liquid Liquid Liquid Liquid Liquid Liquid liquid phase phase phase phase phase phase phase flow output output output output output output through through through through through through 1A02 2A02 3A02 4A02 5A02 6A02 825 Kg/h 600 Kg/h 575 Kg/h 450 Kg/h 340 Kg/h 330 Kg/h Low-pressure Low-pressure Low-pressure Low-pressure Low-pressure Low-pressure Low-pressure steam flow steam steam steam steam steam steam flow into flow into flow into flow into flow into flow into 1 C 2 C 3 C 4 C 5 C 6 C 825 Kg/h 600 Kg/h 575 Kg/h 400 Kg/h 340 Kg/h 330 Kg/h Waste liquid Waste Waste Waste Waste Waste Waste flow liquid liquid liquid liquid liquid liquid through through through through through through 1A01 2A01 3A01 4A01 5A01 6A01  25 Kg/h  25 Kg/h  25 Kg/h  25 Kg/h  10 Kg/h  10 Kg/h (250 ppm) (260 ppm) (270 ppm) (280 ppm) (400 (562 ppm) ppm) Product flow From From From From From Product 2A05 to 3A05 to 4A05 to 5A05 to 6A05 to 130 Kg/h next stage next stage next stage next stage next (1 ppm) 225 Kg/h 200 Kg/h 175 Kg/h 150 Kg/h stage 140 (133.3 (117.5 (95.7 ppm) (65 ppm) Kg/h ppm) ppm) (41.1 ppm) Structural diameter diameter diameter diameter diameter diameter parameters of 800 mm, 600 mm, 600 mm, 400 mm, 400 mm, 200 mm, the distillation height height height height height height column 2500 mm, 2500 mm, 2500 mm, 1500 mm, 1500 mm, 1500 mm, number of number of number of number of number of number of the the the the the the column column column column column column sections sections sections sections sections sections 10. 10. 10. 15. 15. 25. Operating 760 500 240 240 100 80 mmHg pressure at the mmHg mmHg mmHg mmHg mmHg top of the distillation column Operating 100° C. 88° C. 70° C. 70° C. 51° C. 47° C. temperature at the top of the distillation column Operating 900 650 400 500 200 240 pressure at the mmHg mmHg mmHg mmHg mmHg mmHg bottom of the distillation column Operating 104° C. 96° C. 83° C. 88° C. 67° C. 70° C. temperature at the bottom of the distillation column Type of low Roltz Roltz Roltz Roltz Roltz Roltz pressure steam steam steam steam steam steam steam compressor compressor compressor compressor compressor compressor compressor ZQRSR-300 ZQRSR-200 ZQRSR-100 ZQRSR-100 ZQRSR-50 ZQRSR-50 Parameters Inlet 760 500 240 240 100 80 mmHg of pressure mmHg mmHg mmHg mmHg mmHg the Outlet 900 650 400 500 200 200 low- pressure mmHg mmHg mmHg mmHg mmHg mmHg pressure Power  30 KW  20 KW  10 KW  10 KW   5 KW   5 KW steam Adjustable 40-50 Hz 40-50 Hz 40-50 Hz 40-50 Hz 40-50 Hz 40-50 Hz compressors frequency Parameters Heat 1.45 m.sup.2 1.05 m.sup.2 1.01 m.sup.2 0.79 m.sup.2 0.60 m.sup.2 0.59 m.sup.2 of exchange the area liquid Electric   50 KW   40 KW   30 KW   30 KW   20 KW   20 KW phase heating vaporizers power Parameters of Corrugated Corrugated Corrugated Dixon Dixon Dixon the distillation structured structured structured random random random columns mass mass mass mass mass mass transfer transfer transfer transfer transfer transfer stage stage stage stage stage stage element: element: element: element: element: element: Height Height Height Height Height Height equivalent equivalent equivalent equivalent equivalent equivalent to a to a to a to a to a to a theoretical theoretical theoretical theoretical theoretical theoretical plate 6.0 plate 4.5 plate 3.0 plate 3.0 plate plate 1.0 cm cm cm cm 2.0 cm cm Assumed 825 Kg/h 600 Kg/h 575 Kg/h 450 Kg/h 340 Kg/h 330 Kg/h steam vaporized liquid phase flow in use Required heat  495 KW  360 KW  345 KW  270 KW  204 KW  198 KW energy supply Electric power   80 KW   70 KW   40 KW   40 KW   25 KW   25 KW used in the present process System heat 49.5 KW 36.0 KW 34.5 KW   27 KW 20.4 KW 19.8 KW loss 10% taken into consideration Energy saved 73.8% 70.6% 78.4% 75.2% 77.7% 77.4% Notes: the heat of vaporization of water is calculated by 2200 KJ/Kg (0.6 KWh/Kg).

Embodiment 4

(26) Natural water containing the deuterium isotope with an abundance of 150 ppm as feed is fed into the device of the present invention. A two-stage system is connected in series.

(27) The system and operation parameters are shown in table 4.

(28) The flow direction of the stream is the same as that in embodiment 1, and the deuterium depleted water product with a deuterium content of 95 ppm is obtained.

(29) Part of the liquid phase stream in the liquid phase vaporizer nA03 is drained out of the system as waste liquid.

(30) TABLE-US-00004 TABLE 4 Operating parameter table of the two-stage process device of embodiment 4 Operating Parameter First Stage Second Stage Pump Feeding pump S: whirlpool pump 25NPD07Z; Stream delivery pump: whirlpool pump 20NPD07Z. Liquid phase feed flow Feed to 1A05 Feed to 2A05 200 Kg/h (150 ppm) 175 Kg/h (128.6 ppm) Liquid phase return flow Liquid phase return Liquid phase return through 1A07 600 Kg/h through 2A07 250 Kg/h Condensed liquid phase Liquid phase output Liquid phase output flow through 1A02 775 Kg/h through 2A02 400 Kg/h Low-pressure steam flow Low-pressure steam flow Low-pressure steam flow into 1C 775 Kg/h into 2C 400 Kg/h Waste liquid flow Waste liquid through 1A01 Waste liquid through 2A01 25 Kg/h (300 ppm) 25 Kg/h (330 ppm) Product flow From 2A05 to next stage Product 150 Kg/h 175 Kg/h (128.6 ppm) (95 ppm) Structural parameters of diameter 800 mm, height diameter 400 mm, height the distillation column 2500 mm, number of the 1500 mm, number of the column sections 10. column sections 15. Operating pressure at the 100 mmHg 760 mmHg top of the distillation column Operating temperature at 51° C. 100° C. the top of the distillation column Operating pressure at the 200 mmHg 900 mmHg bottom of the distillation column Operating temperature at 67° C. 107° C. the bottom of the distillation column Type of low pressure Roltz steam compressor Roltz steam compressor steam compressor ZQRSR-200 ZQRSR-100 Parameters Inlet 100 mmHg 760 mmHg of the pressure low-pressure Outlet 200 mmHg 900 mmHg steam pressure compressors Power 20 KW 10 KW Adjustable 40-50 Hz 40-50 Hz frequency Parameters Heat 1.36 m.sup.2 0.75 m.sup.2 of the liquid exchange phase area vaporizers Electric 40 KW 20 KW heating power Parameters of the Corrugated structured mass Dixon random mass distillation columns transfer stage element: transfer stage element: Height equivalent to a Height equivalent to a theoretical plate 6.0 cm theoretical plate 4.0 cm Assumed steam 775 Kg/h 425 Kg/h vaporized liquid phase flow in use Required heat energy 465 KW 255 KW supply Electric power used in 60 KW 30 KW the present process System heat loss 10% 46.5 KW 25.5 KW taken into consideration Energy saved 77.1% 78.2% Notes: the heat of vaporization of water is calculated by 2200 KJ/Kg (0.6 KWh/Kg).
The present invention is not limited to the above implementations. Any other alteration, replacement, combination and simplification made without departing from the spirit and the principles of the present invention shall be deemed to be equivalent substitutions and should be encompassed into the scope of protection of the present invention.