CN114349195A - Marine seawater desalination system considering carbon dioxide recovery and working method - Google Patents
Marine seawater desalination system considering carbon dioxide recovery and working method Download PDFInfo
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- CN114349195A CN114349195A CN202210036514.7A CN202210036514A CN114349195A CN 114349195 A CN114349195 A CN 114349195A CN 202210036514 A CN202210036514 A CN 202210036514A CN 114349195 A CN114349195 A CN 114349195A
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Abstract
The invention discloses a marine seawater desalination system considering carbon dioxide recovery and a working method thereof. In the flue gas treatment unit, high-temperature flue gas generated by an internal combustion engine is firstly subjected to oxidation catalytic reduction, a mixture of high-temperature carbon dioxide, nitrogen and water vapor generated after reduction enters an adsorption device for drying after waste heat recovery and cooling, and then enters an air compressor after heat exchange with LNG cold energy through a heat exchanger, wherein a part of high-pressure liquid carbon dioxide is directly collected, the other part of carbon dioxide with pressure enters an energy recovery device for pressure conversion with original seawater to be changed into a gas state again, and then enters the air compressor again to form circulation, and the converted high-pressure seawater forms fresh water through a reverse osmosis membrane. The invention utilizes the critical pressure of the carbon dioxide to perform pressure conversion with the original seawater, so that the original seawater can reach the pressure required by the operation of the reverse osmosis membrane without a high-pressure pump, and the zero-carbon emission and seawater desalination functions of the internal combustion engine are realized.
Description
Technical Field
The invention relates to the field of environmental protection and efficient energy utilization, in particular to a marine seawater desalination system giving consideration to carbon dioxide recovery and a working method.
Background
The seawater desalination plant is divided into a reverse osmosis plant and a seawater distillation plant in principle, and from the point of view of the seawater desalination engineering which has been applied globally, the reverse osmosis membrane method accounts for 65%. In China, by the end of 2018, 103 seawater desalination projects are established nationwide, the scale of produced water exceeds 90 ten thousand meters for cultivation/d, wherein the yield of the reverse osmosis seawater desalination by the membrane method is about 57 ten thousand meters for cultivation/d, accounts for 63.3 percent of the total water yield, and is in absolute dominance. With the commercialization of reverse osmosis desalination technology, the technology is more and more widely applied to ships.
In a reverse osmosis membrane method seawater desalination system, seawater is treated to a predetermined water quality by a pretreatment device, pressurized by a high-pressure pump, and pressure-fed to a reverse osmosis membrane separation device. One part of the pressurized high-pressure seawater overcomes osmotic pressure and passes through the reverse osmosis membrane to become fresh water, and the other part of seawater with increased salt concentration is discharged from the reverse osmosis separation device as concentrated seawater. However, in the reverse osmosis membrane seawater desalination process, because the salt content of seawater is large, and the reverse osmosis process requires large pressure, a large amount of energy is undoubtedly consumed in the seawater desalination process, and the main energy consumption is the pressurization energy consumption of the high-pressure pump on the inflow water, and the operating pressure of the high-pressure pump is usually as high as 5 Mpa-6 Mpa.
In order to reduce the part of energy consumption, in the prior art, the pressure of a pump of a high-pressure pump in a conventional reverse osmosis device is replaced by the hydraulic pressure in the deep sea, so that the seawater desalination is completed, but the method usually needs to install the device in the deep sea with the depth of more than 200 meters, and is difficult to operate and maintain and difficult to implement, so that the development of a system which can replace the high-pressure pump and can recycle the pressure is not slow.
The invention discloses a thermal membrane coupling seawater desalination system, which is named as 'a thermal membrane coupling seawater desalination system' with the application number of 201310002417.7 and is used for reducing the energy consumption of the thermal membrane coupling seawater desalination system. The system comprises a seawater pretreatment unit, a reverse osmosis unit and a low-temperature multi-effect unit, wherein a steam turbine is arranged on a steam inlet pipeline, the steam turbine is connected with a high-pressure pump shaft of the reverse osmosis unit in series, and the high-pressure pump is driven to work by utilizing steam expansion to provide the utilization rate of steam heat energy, so that the electric energy consumed by the high-pressure pump is reduced. In the system, the steam turbine is used for acting to drive the high-pressure pump to work, although the consumed electric energy is reduced, the energy consumption of the steam turbine is increased, and the energy consumption of a reverse osmosis membrane seawater desalination system is not reduced.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a marine seawater desalination system with carbon dioxide recovery, which captures and recovers carbon dioxide generated by an internal combustion engine by using a flue gas treatment unit, and simultaneously performs pressure conversion on critical pressure of the carbon dioxide and seawater to achieve the pressure condition required by reverse osmosis membrane seawater desalination, thereby realizing zero carbon emission of the internal combustion engine and fresh water preparation.
The invention adopts the following technical scheme for realizing the aim of the invention:
a marine seawater desalination system considering carbon dioxide recovery comprises a flue gas treatment unit, an energy conversion unit and a seawater desalination unit;
the flue gas treatment unit comprises: the LNG inlet is connected with the left interface of the LNG pump through a pipeline, the right interface of the LNG pump is connected with the upper interface of the heat exchanger through a pipeline, the lower interface of the heat exchanger is connected with the lower interface of the internal combustion engine through a pipeline, and the internal combustion engine is sequentially connected with the catalytic converter of the flue gas, the waste heat recoverer, the adsorption device and the heat exchanger;
the energy conversion unit includes: the device comprises a gas compressor, a pressure sensor I, a pressure sensor II, a PLC (programmable logic controller), a first electric control valve, a second electric control valve, an expansion valve, a separator, a nitrogen outlet, a liquid carbon dioxide outlet, an energy recovery device I, a check valve, a filter and a raw seawater inlet, wherein a left interface of the gas compressor (8) is connected with the heat exchanger through a pipeline, a right interface of the gas compressor is connected with a lower interface of the pressure sensor I through a pipeline, an upper interface of the pressure sensor I is connected with the PLC through a signal cable, the PLC is simultaneously connected with the first electric control valve and the second electric control valve through signal cables, an upper interface of the first electric control valve is connected with a right interface of the gas compressor through a pipeline, a lower interface of the first electric control valve is connected with the separator through a pipeline, and an upper interface of the separator is the nitrogen outlet, the lower interface of the expansion valve is the liquid carbon dioxide outlet, the pressure sensor II is also connected with the PLC through a signal cable, the left interface of the expansion valve is connected with the lower interface of the pressure sensor I through a pipeline, the right interface of the expansion valve is connected with the lower interface of the pressure sensor II through a pipeline, the upper interface of the second electric control valve is connected with the right interface of the expansion valve through a pipeline, the lower interface of the second electric control valve is connected with the interface a of the energy recovery device I through a pipeline, the interface b of the energy recovery device I is connected with the lower interface of the air compressor through a pipeline, the interface d of the energy recovery device I is connected with the check valve through a pipeline, and the check valve is sequentially connected with the filter and the original seawater inlet through pipelines;
the seawater desalination unit comprises a first-stage reverse osmosis membrane, a c interface of the energy recovery device I is connected with the first-stage reverse osmosis membrane through a pipeline, and a right interface of the first-stage reverse osmosis membrane is connected with the fresh water collecting box through a pipeline.
Preferably, the fuel in the internal combustion engine is natural gas, the heat exchanger is a plate heat exchanger, and a flue gas channel and an LNG channel are arranged in the heat exchanger.
Preferably, a catalyst and a reducing agent are arranged in the flue gas catalytic converter, the catalyst is a metal oxide or a zeolite molecular sieve, and the reducing agent is urea or liquid ammonia.
Preferably, a steam pipeline is arranged in the waste heat recoverer, and waste heat recovery is utilized for heat supply or power generation.
Preferably, an adsorbent is arranged in the adsorption device, and the adsorbent is activated carbon or activated alumina.
Preferably, the nitrogen outlet is provided with a gas storage tank, and the liquid carbon dioxide outlet is provided with a liquid storage tank.
Preferably, the expansion valve is a gas expansion valve, and plays a role in throttling and reducing pressure.
Preferably, still be equipped with second grade reverse osmosis membrane, energy recuperation device II, booster pump and concentrated seawater outlet in the seawater desalination unit, the lower interface of one-level reverse osmosis membrane passes through the pipe connection the c interface of energy recuperation device II, the d interface of energy recuperation device II passes through the pipe connection the left interface of concentrated seawater outlet, the a interface of energy recuperation device II passes through the pipe connection the last interface of filter, the b interface of energy recuperation device II passes through the pipe connection the left interface of booster pump, the right interface of booster pump passes through the pipe connection the left interface of second grade reverse osmosis membrane, the right interface of second grade reverse osmosis membrane passes through the pipe connection the fresh water collecting box.
Preferably, the energy recovery device I and the energy recovery device II are both power exchange type pressure recovery components, a piston is arranged inside the energy recovery device I, two cavities are arranged on the left and right of the piston in the energy recovery device I, and two cavities are arranged on the upper and lower sides of the piston in the energy recovery device II.
Preferably, an energy storage type water wheel is arranged at the lower interface of the second-stage reverse osmosis membrane, and the other interface of the energy storage type water wheel is connected with the compressor shaft.
According to another aspect of the invention, a working method for desalinating seawater for a ship with consideration of carbon dioxide recovery is provided, which specifically comprises the following steps:
(a) the LNG inlet is vaporized through the LNG pump and then supplies power to the internal combustion engine, the flue gas generated by combustion of the internal combustion engine is reduced in the flue gas catalytic converter, the mixture of high-temperature nitrogen, water vapor and carbon dioxide after reduction enters the waste heat recovery device and is cooled to 50-60 ℃ by consumed heat, then the mixture enters the heat exchanger after passing through the adsorption device and is cooled to 25-30 ℃ by cold energy released by vaporization of the LNG, and finally the nitrogen and carbon dioxide gas enter the compressor and increase the pressure to 5-7 Mpa.
(b) When the pressure sensor I detects that the pressure reaches 7Mpa, the PLC drives the first electric control valve to liquefy a part of carbon dioxide and then flow out through a lower interface of the separator, namely the liquid carbon dioxide outlet, and nitrogen flows out through the nitrogen outlet; when the pressure sensor II detects that the pressure of the carbon dioxide passing through the expansion valve is 5-6 Mpa, the PLC drives the second electric control valve to enable the other part of the carbon dioxide with pressure to enter an energy recovery device I, the original seawater enters the filter through the original seawater inlet to remove colloid and suspended impurities in the original seawater, then enters the energy recovery device I through the check valve to perform pressure conversion with the carbon dioxide with pressure, the converted high-pressure liquid carbon dioxide is changed into a gas state again and enters the compressor again, the original seawater enters the primary reverse osmosis membrane after pressure is increased to separate fresh water, and the generated fresh water flows into the fresh water collecting box through a pipeline.
(c) The method comprises the following steps that concentrated seawater with pressure discharged by a first-stage reverse osmosis membrane and original seawater after being shunted by a filter enter an energy recovery device II again for pressure conversion and then are discharged, the discharged concentrated seawater with pressure is pressurized to 5-6 Mpa by a booster pump and enters a second-stage reverse osmosis membrane for separating fresh water, and meanwhile, the high-pressure concentrated seawater discharged by the second-stage reverse osmosis membrane drives an energy storage type water wheel to rotate to do work for the air compressor to work.
By adopting the technical scheme, the invention at least comprises the following beneficial effects:
1. according to the invention, through the coupling of the flue gas treatment unit and the energy conversion unit, the critical pressure of the carbon dioxide is efficiently utilized, the pressure leakage is avoided, the energy recycling is enhanced, and the liquid carbon dioxide is collected while the fresh water is prepared. In the energy conversion device, the carbon dioxide after pressure conversion with the original seawater enters the compressor again for circulation, so that the environmental pollution caused by direct discharge is avoided, the recovery rate of the carbon dioxide is improved, and the recovery rate can reach over 90 percent.
2. According to the invention, the energy conversion unit performs pressure conversion with the original seawater in the energy recovery device by using the critical pressure of the carbon dioxide, so that the extra energy consumed by using a high-pressure pump in the traditional reverse osmosis membrane seawater desalination system is avoided, and the power consumption can be reduced by 30%.
3. The invention directly captures carbon dioxide generated during combustion of natural gas by using LNG cold energy and seawater cold energy, does not need secondary refrigerant, has simple and efficient system and realizes zero carbon emission of the internal combustion engine.
4. The invention drives the compressor to work by applying work to the concentrated seawater with high pressure discharged by the secondary osmotic membrane through the energy storage type water wheel, thereby reducing the additional driving energy consumption of the compressor to a certain extent.
Drawings
FIG. 1 is a schematic diagram of the structural principle of a marine seawater desalination system with consideration of carbon dioxide recovery according to the present invention.
Reference numerals: the device comprises an LNG inlet 1, an LNG pump 2, an internal combustion engine 3, a flue gas catalytic converter 4, a waste heat recoverer 5, an adsorption device 6, a heat exchanger 7, a compressor 8, a pressure sensor I9, a pressure sensor II10, a first electric control valve 11, a second electric control valve 12, an expansion valve 13, an energy recovery device I14, an energy recovery device II15, a primary reverse osmosis membrane 16, a secondary reverse osmosis membrane 17, a booster pump 18, an energy storage type water wheel 19, a raw seawater inlet 20, a filter 21, a check valve 22, a concentrated seawater outlet 23, a fresh water collecting tank 24, a nitrogen outlet 25, a liquid carbon dioxide outlet 26, a separator 27 and a PLC (programmable logic controller) 28.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be described in further detail below with reference to the drawings in the embodiments of the present invention. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
As shown in fig. 1, a marine seawater desalination system and a working method thereof with consideration of carbon dioxide recovery comprise a flue gas treatment unit, an energy conversion unit and a seawater desalination unit.
Wherein the flue gas treatment unit comprises: the LNG system comprises an LNG inlet 1, an LNG pump 2, an internal combustion engine 3, a flue gas catalytic converter 4, a waste heat recoverer 5, an adsorption device 6 and a heat exchanger 7, wherein the LNG inlet 1 is connected with a left connector of the LNG pump 2 through a pipeline, a right connector of the LNG pump 2 is connected with an upper connector of the heat exchanger 7 through a pipeline, a lower connector of the heat exchanger 7 is connected with a lower connector of the internal combustion engine 3 through a pipeline, LNG is vaporized through the LNG pump 2 and then is supplied to the internal combustion engine 3 to do work, the internal combustion engine 3 is sequentially connected with the flue gas catalytic converter 4, the waste heat recoverer 5, the adsorption device 6 and the heat exchanger 7 through pipelines, so that flue gas generated by the internal combustion engine 3 is reduced in the flue gas converter 4, a mixture of nitrogen, water vapor and carbon dioxide with high temperature after reduction is cooled to 50-60 ℃ by consumed heat in the waste heat recoverer 5, and enters the heat exchanger 7 after being adsorbed by an adsorbent in the adsorption device 6 to be vaporized and cooled secondarily by cold energy released by LNG, cooling to 25-30 ℃, wherein the adsorbent is activated carbon or activated alumina, a catalyst and a reducing agent are arranged in the flue gas catalytic converter 4, the catalyst is a metal oxide or a zeolite molecular sieve, and the reducing agent is urea or liquid ammonia.
The heat exchanger 7 is a plate heat exchanger, a flue gas channel and an LNG channel are arranged in the heat exchanger 7, and compared with a shell-and-tube heat exchanger, the heat transfer coefficient of the plate heat exchanger is generally 2-3 times higher under the condition of the same pressure loss.
Meanwhile, a steam pipeline is arranged in the waste heat recoverer 5, and heat supply or power generation is performed by waste heat recovery.
The energy conversion unit includes: the system comprises a compressor 8, a pressure sensor I9, a pressure sensor II10, a PLC 28, a first electric control valve 11, a second electric control valve 12, an expansion valve 13, a separator 27, a nitrogen outlet 25, a liquid carbon dioxide outlet 26, an energy recovery device I14, a check valve 22, a filter 21 and a raw seawater inlet 20;
as shown in fig. 1, the left port of the compressor 8 is connected to the right port of the heat exchanger 7 through a pipeline, the right port of the compressor 8 is connected to the lower port of the pressure sensor I9 through a pipeline, the upper port of the pressure sensor I9 is connected to the left lower port of the PLC controller 28 through a signal cable, the left port of the PLC controller 28 is connected to the right port of the first electric control valve 11 through a signal cable, the upper port of the first electric control valve 11 is connected to the right port of the compressor 8 through a pipeline, the lower port of the first electric control valve 11 is connected to the left port of the separator 27 through a pipeline, the upper port of the separator 27 is the nitrogen outlet 25, the lower port of the separator 27 is the liquid carbon dioxide outlet 26, the left port of the expansion valve 13 is connected to the lower port of the pressure sensor I9 through a pipeline, the right interface of the expansion valve 13 is connected with the lower interface of the pressure sensor II10 through a pipeline, the upper interface of the pressure sensor II10 is connected with the right lower interface of the PLC 28 through a signal cable, the right interface of the PLC 28 is connected with the right interface of the second electric control valve 12 through a signal cable, the upper interface of the second electric control valve 12 is connected with the right interface of the expansion valve 13 through a pipeline, wherein the expansion valve 13 is a gas expansion valve and plays a role in throttling and pressure reduction, the lower interface of the second electric control valve 12 is connected with the interface a of the energy recovery device I14 through a pipeline, the interface b of the energy recovery device I14 is connected with the lower interface of the compressor 8 through a pipeline, the interface d of the energy recovery device I14 is connected with the upper interface of the check valve 22 through a pipeline, the lower interface of the check valve 22 is connected with the upper interface of the filter 21 through a pipeline, the lower port of the filter 21 is connected with the raw seawater inlet 20 through a pipeline.
A gas storage tank is arranged at the nitrogen outlet 25, and a liquid storage tank is arranged at the liquid carbon dioxide outlet 26 for recovering nitrogen and liquid carbon dioxide.
The energy recovery device I14 is a power exchange type pressure recovery part, a piston is arranged in the energy recovery device I14, two cavities are arranged on the left and right of the piston, and when high-pressure liquid carbon dioxide enters the left cavity, the piston is pushed to move rightwards, so that the seawater pressure is increased.
The seawater desalination unit comprises: one-level reverse osmosis membrane 16, two-level reverse osmosis membrane 17, energy storage formula water wheels 19, energy recuperation device II15, booster pump 18, concentrated seawater export 23, fresh water collecting box 24, the left interface of one-level reverse osmosis membrane 16 passes through the pipe connection the c interface of energy recuperation device I14, the right interface of one-level reverse osmosis membrane 16 passes through the pipe connection fresh water collecting box 24, the lower interface of one-level reverse osmosis membrane 16 passes through the pipe connection the c interface of energy recuperation device II15, will pass through the concentrated seawater that has pressure of reverse osmosis membrane and recycle, the d interface of energy recuperation device II15 passes through the pipe connection the left interface of concentrated seawater export 23, the a interface of energy recuperation device II15 passes through the pipe connection the last interface of filter 21, the b interface of energy recuperation device II15 passes through the pipe connection the left interface of booster pump 18, the right connector of the booster pump 18 is connected with the left connector of the secondary reverse osmosis membrane 17 through a pipeline, and the right connector of the secondary reverse osmosis membrane 17 is connected with the fresh water collecting box 24 through a pipeline.
The lower interface of the secondary reverse osmosis membrane 17 is provided with an energy storage type water wheel 19, and the other interface of the energy storage type water wheel 19 is connected with the compressor 8, so that high-pressure concentrated seawater discharged by the secondary reverse osmosis membrane 17 drives the energy storage type water wheel 19 to rotate to apply work so as to store electric energy for the compressor 8 to work.
The energy recovery device II15 is a power exchange type pressure recovery part, a piston is arranged in the energy recovery device II15, two cavities are arranged above and below the piston, and when high-pressure liquid carbon dioxide enters the left cavity, the piston is pushed to move rightwards so as to lift the pressure of seawater.
The nitrogen and carbon dioxide gas produced by the flue gas treatment system enter the gas compressor 8 to increase the pressure to 5-7 Mpa, when the pressure sensor I9 detects that the pressure reaches 7Mpa, the PLC 28 drives the first electric control valve 11 to liquefy part of the carbon dioxide and then flow out through the lower interface of the separator 27, namely the liquid carbon dioxide outlet 26, the nitrogen flows out through the nitrogen outlet 25, when the pressure sensor II10 detects that the pressure of the carbon dioxide passing through the expansion valve 13 is 5-6 Mpa, the PLC 28 drives the second electric control valve 12 to make the other part of the carbon dioxide with pressure enter the energy recovery device I14, the raw seawater enters the filter 21 through the raw seawater inlet 20 to remove colloid and suspended impurities in the raw seawater, and then enters the energy recovery device I14 through the check valve 22 to perform pressure conversion with the carbon dioxide with pressure, the high-pressure liquid carbon dioxide is changed into a gas state again and enters the gas compressor 8 again, the pressure of the original seawater is increased and then enters the first-stage reverse osmosis membrane 16 to separate fresh water, and the generated fresh water flows into the fresh water collecting box 24 through a pipeline.
Generally, the pressure of the concentrated seawater discharged by the first-stage reverse osmosis membrane 16 can reach 4.8Mpa to 5.8Mpa, the concentrated seawater with the pressure and the original seawater which is split by the filter 21 enter the energy recovery device II15 again for pressure conversion and then are discharged, the discharged concentrated seawater with the pressure is pressurized to 5Mpa to 6Mpa by the booster pump 18 and enters the second-stage reverse osmosis membrane 17 to be separated into fresh water, and the high-pressure concentrated seawater discharged by the second-stage reverse osmosis membrane 17 drives the energy storage type water wheel 19 to rotate to do work to supply the compressor 8 to work, so that the cycle is performed.
The above description is only exemplary of the present invention and should not be taken as limiting the invention, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "left", "right", "inner", "outer", etc. indicate positional relationships based on those shown in the drawings, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the elements referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Claims (10)
1. The utility model provides a compromise marine sea water desalination of carbon dioxide recovery system which characterized in that, includes flue gas processing unit, energy conversion unit and sea water desalination unit, flue gas processing unit includes: the LNG system comprises an LNG inlet (1), an LNG pump (2), an internal combustion engine (3), a flue gas catalytic converter (4), a waste heat recoverer (5), an adsorption device (6) and a heat exchanger (7), wherein the LNG inlet (1) is connected with a left interface of the LNG pump (2) through a pipeline, a right interface of the LNG pump (2) is connected with an upper interface of the heat exchanger (7) through a pipeline, a lower interface of the heat exchanger (7) is connected with a lower interface of the internal combustion engine (3) through a pipeline, and the internal combustion engine (3) is sequentially connected with the flue gas catalytic converter (4), the waste heat recoverer (5), the adsorption device (6) and the heat exchanger (7);
the energy conversion unit includes: the device comprises a gas compressor (8), a pressure sensor I (9), a pressure sensor II (10), a PLC (28), a first electric control valve (11), a second electric control valve (12), an expansion valve (13), a separator (27), a nitrogen outlet (25), a liquid carbon dioxide outlet (26), an energy recovery device I (14), a check valve (22), a filter (21) and a raw seawater inlet (20), wherein a left interface of the gas compressor (8) is connected with the heat exchanger (7) through a pipeline, a right interface of the gas compressor (8) is connected with a lower interface of the pressure sensor I (9) through a pipeline, an upper interface of the pressure sensor I (9) is connected with the PLC (28) through a signal cable, and the PLC (28) is simultaneously connected with the first electric control valve (11) and the second electric control valve (12) through signal cables respectively, the last interface of first electric control valve (11) passes through the pipe connection the right interface of compressor (8), the lower interface of first electric control valve (11) passes through the pipe connection separator (27), the last interface of separator (27) does nitrogen gas export (25), and its lower interface does liquid carbon dioxide export (26), pressure sensor II (10) still with PLC controller (28) pass through signal cable connection, the left interface of expansion valve (13) passes through the pipe connection the lower interface of pressure sensor I (9), the right interface of expansion valve (13) passes through the pipe connection the lower interface of pressure sensor II (10), the last interface of second electric control valve (12) passes through the pipe connection the right interface of expansion valve (13), the lower interface of second electric control valve (12) passes through the pipe connection the a interface of energy recuperation device I (14), the b interface of the energy recovery device I (14) is connected with the lower interface of the compressor (8) through a pipeline, the d interface of the energy recovery device I (14) is connected with the check valve (22) through a pipeline, and the check valve (22) is sequentially connected with the filter (21) and the raw seawater inlet (20) through pipelines;
the seawater desalination unit comprises a first-stage reverse osmosis membrane (16), a c interface of the energy recovery device I is connected with the first-stage reverse osmosis membrane (16) through a pipeline, and a right interface of the first-stage reverse osmosis membrane (16) is connected with the fresh water collecting box (24) through a pipeline.
2. The seawater desalination system for ships with consideration of carbon dioxide recovery as recited in claim 1, wherein the fuel in the internal combustion engine (3) is natural gas, the heat exchanger (7) is a plate heat exchanger, and a flue gas channel and an LNG channel are arranged in the heat exchanger (7).
3. The seawater desalination system for ships with consideration of carbon dioxide recovery as recited in claim 1, wherein a catalyst and a reducing agent are provided in the flue gas catalytic converter (4), the catalyst is a metal oxide or a zeolite molecular sieve, and the reducing agent is urea or liquid ammonia; and a steam pipeline is arranged in the waste heat recoverer (5).
4. The seawater desalination system for ships with consideration of carbon dioxide recovery as recited in claim 1, wherein the adsorption device (6) is provided with an adsorbent, and the adsorbent is activated carbon or activated alumina.
5. The seawater desalination system for ships with consideration of carbon dioxide recovery as recited in claim 1, wherein the nitrogen outlet (25) is provided with a gas storage tank, and the liquid carbon dioxide (26) outlet is provided with a liquid storage tank.
6. The seawater desalination system for ships with consideration of carbon dioxide recovery as recited in claim 1, wherein the expansion valve (13) is a gas expansion valve.
7. The marine seawater desalination system for recovering carbon dioxide as claimed in any one of claims 1 to 6, wherein a secondary reverse osmosis membrane (17), an energy recovery device II (15), a booster pump (18) and a concentrated seawater outlet (23) are further arranged in the seawater desalination unit, a lower interface of the primary reverse osmosis membrane (16) is connected with an interface c of the energy recovery device II (15) through a pipeline, an interface d of the energy recovery device II (15) is connected with the concentrated seawater outlet (23) through a pipeline, an interface a of the energy recovery device II (15) is connected with an upper interface of the filter (21) through a pipeline, an interface b of the energy recovery device II (15) is connected with a left interface of the booster pump (18) through a pipeline, a right interface of the booster pump (18) is connected with a left interface of the secondary reverse osmosis membrane (17) through a pipeline, the right connector of the secondary reverse osmosis membrane (17) is connected with the fresh water collecting box (24) through a pipeline.
8. The seawater desalination system for ships with consideration on carbon dioxide recovery as recited in claim 7, wherein the energy recovery device I (14) and the energy recovery device II (15) are both power exchange type pressure recovery components, a piston is disposed inside the energy recovery device I (14), two cavities are disposed on left and right sides of the piston in the energy recovery device I (14), and two cavities are disposed on upper and lower sides of the piston in the energy recovery device II (15).
9. The seawater desalination system for ships with consideration on carbon dioxide recovery as recited in claim 7, wherein an energy storage water wheel (19) is arranged at a lower interface of the secondary reverse osmosis membrane (17), and another interface of the energy storage water wheel (19) is connected with the shaft of the compressor (8).
10. A marine seawater desalination working method considering carbon dioxide recovery is characterized by specifically comprising the following steps:
(a) the LNG inlet (1) is vaporized by the LNG pump (2) and then supplies to the internal combustion engine (3) to do work, flue gas generated by combustion of the internal combustion engine (3) is reduced in the flue gas catalytic converter (4), the mixture of high-temperature nitrogen, water vapor and carbon dioxide after reduction enters the waste heat recoverer (5) to be cooled to 50-60 ℃ by consumed heat, then enters the heat exchanger (7) after water vapor is absorbed by the absorption device (6) and is cooled to 25-30 ℃ with cold energy released by vaporization of LNG for secondary cooling, and finally nitrogen and carbon dioxide gas enter the compressor (8) to increase the pressure to 5-7 Mpa;
(b) when the pressure sensor I (9) detects that the pressure reaches 7Mpa, the PLC controller (28) drives the first electric control valve (11) to liquefy a part of carbon dioxide and then flow out through a lower port of the separator (27), namely the liquid carbon dioxide outlet (26), and nitrogen flows out through the nitrogen outlet (25); when the pressure sensor II (10) detects that the pressure of the carbon dioxide passing through the expansion valve (13) is 5-6 Mpa, the PLC controller (28) drives the second electric control valve (12) to enable the other part of the carbon dioxide with pressure to enter an energy recovery device I (14), the raw seawater enters the filter (21) through the raw seawater inlet (20) to remove colloid and suspended impurities in the raw seawater, then enters the energy recovery device I (14) through the check valve (22) to be subjected to pressure conversion with the carbon dioxide with pressure, the converted high-pressure liquid carbon dioxide is changed into a gas state again and enters the air compressor (8), the raw seawater is subjected to pressure lifting and then enters the first-stage reverse osmosis membrane (16) to separate fresh water, and the generated fresh water flows into the fresh water collecting box (24) through a pipeline;
(c) the concentrated seawater with pressure discharged by the first-stage reverse osmosis membrane (16) and the original seawater after being shunted by the filter (21) enter the energy recovery device II (15) again for pressure conversion and then are discharged, the discharged concentrated seawater with pressure is pressurized to 5 Mpa-6 Mpa by the booster pump (18) and enters the second-stage reverse osmosis membrane (17) to separate fresh water, and meanwhile, the high-pressure concentrated seawater discharged by the second-stage reverse osmosis membrane (17) drives the energy storage type water wheel (19) to rotate to do work for the work of the air compressor (8).
Priority Applications (1)
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114909605A (en) * | 2022-06-08 | 2022-08-16 | 江苏科技大学 | LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof |
| CN115610635A (en) * | 2022-10-24 | 2023-01-17 | 大连海事大学 | Energy management system for production, storage and carbon capture of low-temperature liquid goods |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004081913A (en) * | 2002-08-23 | 2004-03-18 | Hitachi Zosen Corp | Sea water desalinating method by reverse osmosis |
| DE202004003175U1 (en) * | 2004-03-01 | 2004-07-08 | Schmid, Heinrich | Sea water desalination plant operated by liquid nitrogen, has evaporator pressurizing reverse osmosis unit and employs liberated gas to drive control equipment and liquids |
| US20100192575A1 (en) * | 2007-09-20 | 2010-08-05 | Abdulsalam Al-Mayahi | Process and systems |
| CN103058438A (en) * | 2013-01-05 | 2013-04-24 | 中国电子工程设计院 | Hot film coupling seawater desalination system |
| US20150298062A1 (en) * | 2012-07-31 | 2015-10-22 | Ronghui Zhu | Membrane seawater desalination pressurization and energy recovery integrated method and device |
| CN105152399A (en) * | 2015-09-01 | 2015-12-16 | 中冶建筑研究总院有限公司 | Reverse osmosis container-type sea water desalination plant and water producing process thereof |
| CN109305720A (en) * | 2018-11-26 | 2019-02-05 | 西安交通大学 | A kind of reverse osmosis seawater desalination system of two-stage hydraulic recovery and process for desalinating seawater based on it |
| CN110332764A (en) * | 2019-05-27 | 2019-10-15 | 江苏科技大学 | It is a kind of to recycle CO using LNG cold energy step combined-circulation2Zero-emission dynamical system |
| CN110563089A (en) * | 2019-08-05 | 2019-12-13 | 江苏科技大学 | High-pressure energy recovery device for reverse osmosis seawater desalination system |
-
2022
- 2022-01-13 CN CN202210036514.7A patent/CN114349195B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004081913A (en) * | 2002-08-23 | 2004-03-18 | Hitachi Zosen Corp | Sea water desalinating method by reverse osmosis |
| DE202004003175U1 (en) * | 2004-03-01 | 2004-07-08 | Schmid, Heinrich | Sea water desalination plant operated by liquid nitrogen, has evaporator pressurizing reverse osmosis unit and employs liberated gas to drive control equipment and liquids |
| US20100192575A1 (en) * | 2007-09-20 | 2010-08-05 | Abdulsalam Al-Mayahi | Process and systems |
| US20150298062A1 (en) * | 2012-07-31 | 2015-10-22 | Ronghui Zhu | Membrane seawater desalination pressurization and energy recovery integrated method and device |
| CN103058438A (en) * | 2013-01-05 | 2013-04-24 | 中国电子工程设计院 | Hot film coupling seawater desalination system |
| CN105152399A (en) * | 2015-09-01 | 2015-12-16 | 中冶建筑研究总院有限公司 | Reverse osmosis container-type sea water desalination plant and water producing process thereof |
| CN109305720A (en) * | 2018-11-26 | 2019-02-05 | 西安交通大学 | A kind of reverse osmosis seawater desalination system of two-stage hydraulic recovery and process for desalinating seawater based on it |
| CN110332764A (en) * | 2019-05-27 | 2019-10-15 | 江苏科技大学 | It is a kind of to recycle CO using LNG cold energy step combined-circulation2Zero-emission dynamical system |
| CN110563089A (en) * | 2019-08-05 | 2019-12-13 | 江苏科技大学 | High-pressure energy recovery device for reverse osmosis seawater desalination system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114909605A (en) * | 2022-06-08 | 2022-08-16 | 江苏科技大学 | LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof |
| CN114909605B (en) * | 2022-06-08 | 2024-04-19 | 江苏科技大学 | LNG ship cold energy circulating storage and cold energy comprehensive utilization system and working method thereof |
| CN115610635A (en) * | 2022-10-24 | 2023-01-17 | 大连海事大学 | Energy management system for production, storage and carbon capture of low-temperature liquid goods |
| CN115610635B (en) * | 2022-10-24 | 2023-11-17 | 大连海事大学 | Energy management system for production, storage and carbon capture of low-temperature liquid cargo products |
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