CN114477344B - Sea water desalination device by waste heat of jet device waste gas - Google Patents
Sea water desalination device by waste heat of jet device waste gas Download PDFInfo
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- CN114477344B CN114477344B CN202011268190.7A CN202011268190A CN114477344B CN 114477344 B CN114477344 B CN 114477344B CN 202011268190 A CN202011268190 A CN 202011268190A CN 114477344 B CN114477344 B CN 114477344B
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- flue gas
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Water Supply & Treatment (AREA)
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- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The application discloses an intelligent descaling heat exchanger and a seawater desalination device, wherein the heat exchanger comprises a shell, a heat pipe and a division plate, wherein the heat pipe and the division plate are arranged in the shell, the division plate divides the heat pipe into a hot end positioned at the upper part and a cold end positioned at the lower part; when the sensor detects that the scaling amount is still at a higher value after a plurality of times of flushing, the controller controls the valve of the descaling agent storage tank to be opened, and the descaling agent is sprayed onto the o-heat pipe through the spraying device. According to the intelligent descaling heat exchanger provided by the application, different descaling modes are adopted according to different conditions, so that the intelligent descaling degree of the system is improved.
Description
Technical Field
The application belongs to the field of heat exchangers, and particularly provides a seawater desalination device taking flue gas as a desalination heat source under the use condition of ships
Background
The heat exchanger is widely applied to industries such as chemical industry, petroleum, refrigeration, nuclear energy, power and the like, and the demand for the heat exchanger in industrial production is increased and the quality requirement for the heat exchanger is also increased due to the worldwide energy crisis so as to reduce energy consumption. In recent decades, although compact heat exchangers (plate-type, plate-fin-type, pressure-welded plate-type heat exchangers, etc.), heat pipe-type heat exchangers, direct contact heat exchangers, etc. have been rapidly developed, shell-and-tube heat exchangers still occupy the dominant position of yield and usage due to high reliability and wide adaptability, and the usage of the shell-and-tube heat exchangers in the current industrial devices still accounts for about 70% of the usage of all heat exchangers according to relevant statistics.
At present, the sea water desalination technology mainly comprises a thermal method and a membrane method, wherein the thermal method is represented by a multi-effect distillation Method (MEE) and a multi-stage flash evaporation Method (MSF), and the membrane method is represented by an RO reverse osmosis method; the multi-effect distillation method makes the whole heat utilization rate higher by recycling the steam heat, but the device is huge in volume due to the existence of the multi-effect evaporator and is usually built on coastal land to produce fresh water; the multistage flash evaporation method is characterized in that the multistage flash evaporation method is to heat seawater firstly, then to introduce the seawater into a distillation tank with gradually reduced pressure, and to perform gradual distillation by utilizing the characteristic that the boiling point of the water is reduced along with the reduction of the pressure, wherein the heating and the distillation are separately performed, so that the scaling of the seawater is effectively reduced, but the energy consumption is higher and the volume is larger due to the need of a negative pressure device; the RO reverse osmosis method is to pressurize seawater through the semipermeable membrane to make the water molecules permeate the semipermeable membrane by utilizing the pressure difference principle to finish the separation of water and salt, and has high desalination efficiency and stable work, so the RO reverse osmosis method is widely popularized, but the energy source has high use cost for the limited use scene carried by the energy source of the ship due to the high-grade electric energy.
The main engine of the ship is a diesel engine, only 45-50% of the heat generated by the combustion of the fuel oil in the diesel engine is converted into mechanical energy, and about 50% of the energy released by the combustion is dissipated as waste heat, wherein about 25-30% of the heat is taken away by the waste gas, and a large amount of waste heat is directly discharged into the air, so that not only is the energy waste caused, but also the environmental pollution is caused.
Because a large amount of low-grade heat energy in the flue gas exhausted by the ship main engine is not utilized, and meanwhile, a direct heat source is needed to provide desalination energy in the device adopting a thermal method as a sea water desalination principle, the idea of taking ship waste gas as a desalination heat source is generated, and the device is designed by combining the advantages and the characteristics of a multi-effect distillation method and a multi-stage flash evaporation method.
In a sea water desalination plant, a heat exchanger is commonly used as a very common device. However, the existing heat exchanger has the problem of low descaling efficiency in the sea water desalination application. Therefore, the application improves the heat exchanger, so that the heat exchanger is suitable for sea water desalination application.
Disclosure of Invention
The application aims to provide a heat source for a sea water desalination device based on a multi-effect distillation method by utilizing waste heat in smoke discharged by a ship, and produce fresh water on the ship with high efficiency and energy conservation.
The technical scheme of the application is as follows: the heat exchanger comprises a shell, and a heat pipe and a partition plate which are arranged in the shell, wherein the partition plate divides the heat pipe into a hot end positioned at the upper part and a cold end positioned at the lower part, and the heat exchanger is characterized in that smoke enters the lower part of the partition plate, seawater is sprayed above the partition plate, the partition plate is obliquely arranged downwards along the flow direction of the smoke, the upper surface of the partition plate is engraved with discharged lines of bitter water, and a bitter water outlet is positioned on the shell close to the lower end of the inclined plate and above the partition plate.
Preferably, the partition plate has two layers and is made of stainless steel, and the space between the two plates is filled with a heat insulating material.
Preferably, the heat exchanger shell is square, round corners are led at the periphery, the heat exchanger shell is made of single-layer double-phase stainless steel, and the outer part is coated with composite silicate heat-insulating paint; the upper end sealing cover can be detached.
The utility model provides an intelligent descaling heat exchanger, the heat exchanger includes casing and sets up heat pipe and division board in the casing, and the division board separates the heat pipe into the hot junction that is located upper portion and the cold junction that is located the lower part, and characterized in that, flue gas gets into the division board below, and the sea water sprays the division board top, the heat exchanger still includes the detergent holding vessel, and the detergent holding vessel is located the top of heat exchanger, and inside stores the detergent to link to each other through the valve with spray set, set up diffuse reflection fiber sensor in the heat exchanger, when the device normally operates, the diffuse reflection fiber sensor, the scale deposit condition on the perception heat pipe, when the scale deposit volume of detection is too big, increase the spray volume of sea water, erode the heat pipe to open bitter water discharge valve simultaneously; when the sensor detects that the scaling amount is still at a higher value after a plurality of times of flushing, the controller controls the valve of the descaling agent storage tank to be opened, and the descaling agent is sprayed onto the o-heat pipe through the spraying device.
Preferably, the scale remover is polyaspartic acid scale remover and is connected with the lower spray device.
Preferably, when the detected scaling amount is too large, the spraying amount of the seawater is increased, and the heat pipe is washed for a plurality of times.
Preferably, the shell-and-tube heat exchanger is vertically arranged above the fresh water bin, seawater is introduced into the shell, vapor distilled in the two-effect distiller is sucked into the tube, the vapor is liquefied in the tube and flows into the fresh water bin below, meanwhile, the seawater in the shell is preheated, and the preheated seawater enters the one-effect distiller and the two-effect distiller through the spraying device.
Preferably, the device further comprises a spray pipeline, wherein the inlet of the spray pipeline is connected with the seawater outlet of the shell-and-tube heat exchanger, and the outlet of the spray pipeline is connected with the one-effect distiller and the two-effect distiller.
Preferably, the device also comprises a scale remover storage tank, wherein the scale remover storage tank is positioned above the first-effect distiller (1) and the second-effect distiller (2), is internally stored with a scale remover and is connected with the spraying device.
Preferably, the device comprises a Venturi ejector which is arranged on a spray pipeline of the one-effect distiller, and the air extraction end is connected with a fresh water bin.
Preferably, the evaporator comprises a foam-catching net which is arranged on a pipeline between the hot end of the first-effect distiller and the cold end of the second-effect distiller and on a pipeline between the hot end of the second-effect distiller and the shell-and-tube heat exchanger.
Preferably, a flue gas filter is included, which is arranged in front of the inlet of the flue gas into the one-effect distiller.
Preferably, the device comprises a temperature equalizing device, wherein the temperature equalizing device is arranged on a pipeline for flue gas to enter the one-effect distiller.
The beneficial effects of the application are as follows:
1. according to the intelligent descaling heat exchanger provided by the application, different descaling modes are adopted according to different conditions, so that the intelligent descaling degree of the system is improved.
2. The separation plate in the heat exchanger provided by the application has the characteristics of reducing and accelerating the flue gas below by inclined arrangement, so that the flue gas flows more smoothly; and simultaneously, the upper surface is combined with the carved lines so that the bitter water can be discharged more smoothly.
3. According to the double-effect reduced pressure distillation device integrating multiple-effect distillation and multi-stage flash evaporation method thought, the heat of the smoke is absorbed in the first effect to distill seawater, distilled vapor is led into the double-effect distiller, and on one hand, the vapor releases the liquefied latent heat to the heat pipe, and on the other hand, the vapor is liquefied into fresh water; the vapor distilled in the double-effect distiller exchanges heat with the shell-and-tube heat exchanger, and simultaneously liquefies into fresh water, and releases the liquefied latent heat to untreated seawater to play a role of preheating; therefore, the device utilizes the heat energy of the waste flue gas as a heat source for desalination, improves the utilization efficiency of the energy of the internal combustion engine, fully utilizes the heat energy transferred to the water vapor, and greatly improves the utilization efficiency of the heat energy through the complementary relationship of liquefying, releasing heat, evaporating and absorbing heat.
4. The venturi tube ejector provided by the application is used in a seawater spraying pipeline, so that the negative pressure requirement in the device can be realized by flowing seawater, the requirement of the negative pressure distillation in the double-effect distiller is met, the use of a high-power vacuum pump is avoided, and the energy consumption is reduced; simultaneously, the pressure in the spraying pipeline can be increased by the pumped air, the flow speed of the sprayer in the first-effect distiller is larger, and the seawater atomization effect is better.
5. The chemical scale remover provided by the application is polyaspartic acid, is an environment-friendly scale inhibitor, and enables inorganic salt to be easily separated from the surface of an object through chelation dissolution and lattice distortion, so that the chemical scale remover has strong scale inhibition capability, is nontoxic and harmless, can be automatically degraded in the environment, and does not pollute the environment.
6. The application provides a novel temperature equalizing device, which is characterized in that a flow guiding plate is arranged in a flue gas pipe, so that a part of flue gas is guided to the opposite direction along the flow guiding plate and is fully mixed with flue gas entering in the opposite direction, the temperature uniformity of the flue gas is realized, the further heat exchange requirement is realized, and the service life of a product is prolonged.
Drawings
FIG. 1 is a schematic view of the principle of the apparatus of the present application
FIG. 2 is an isometric view of a three-dimensional model of the present application
FIG. 3 is an axial sectional view of a smoke tube provided with a drainage plate according to the application;
fig. 4 is a schematic view of the dimensions of the smoke tube setup drainage plate of the present application.
Fig. 5 is a schematic perspective view of 1 drainage plate per layer.
Fig. 6 is a schematic perspective view of 3 drainage plates per layer.
Detailed Description
The following will make additional description on the technical solution in the embodiment of the present application with reference to the drawings in the embodiment of the present application.
The sea water desalination device based on ship waste gas waste heat is shown in figure 1, the device comprises a first-effect distiller 1, a second-effect distiller 2, a shell-and-tube heat exchanger 3 and a fresh water bin 4, wherein the first-effect distiller 1 is connected with the second-effect distiller 2, the second-effect distiller 2 is connected with the shell-type heat exchanger 3, the fresh water bin 4 is arranged at the lower parts of the second-effect distiller 2 and the shell-and-tube heat exchanger 3, a first-effect heat pipe 11 and a first-effect separation plate 13 are arranged in the first-effect distiller 1, the first-effect separation plate 13 separates the first-effect heat pipe 11 into a hot end positioned at the upper part and a cold end positioned at the lower part, a second-effect heat pipe 21 and a second-effect separation plate are arranged in the second-effect distiller 2, the second-effect separation plate separates the second-effect heat pipe into the hot end positioned at the upper part and the cold end positioned at the lower part, the flue gas is introduced into the cold end of the first effect distiller 1, the heat of the flue gas is transferred to the upper hot end through the cold end of the high-temperature heat pipe 11, the sprayed cold sea water is distilled, the vapor distilled by the first effect distiller 1 is guided into the cold end of the second effect distiller 2, on one hand, the vapor is liquefied into fresh water when meeting cold and flows into the lower fresh water bin 4, on the other hand, the liquefied latent heat of the vapor is transferred to the upper hot end of the second effect heat pipe 21 through the second effect heat pipe 21, the sprayed sea water of the second effect distiller 2 is distilled, the vapor distilled by the second effect distiller 2 enters the shell-and-tube heat exchanger 3, the heat exchange is carried out between the vapor and the cold sea water in the shell-and-tube heat exchanger 3, and the vapor is liquefied into fresh water when preheating the sea water and flows into the lower fresh water bin 4.
According to the double-effect reduced pressure distillation device integrating multiple-effect distillation and multi-stage flash evaporation method thought, the heat of the smoke is absorbed in the first effect to distill seawater, distilled vapor is led into the double-effect distiller, and on one hand, the vapor releases the liquefied latent heat to the heat pipe, and on the other hand, the vapor is liquefied into fresh water; the vapor distilled in the double-effect distiller exchanges heat with the shell-and-tube heat exchanger, and simultaneously liquefies into fresh water, and releases the liquefied latent heat to untreated seawater to play a role of preheating; therefore, the device utilizes the heat energy of the waste flue gas as a heat source for desalination, improves the utilization efficiency of the energy of the internal combustion engine, fully utilizes the heat energy transferred to the water vapor, and greatly improves the utilization efficiency of the heat energy through the complementary relationship of liquefying, releasing heat, evaporating and absorbing heat.
Preferably, the first-effect partition plate 13 and the second-effect partition plate have two layers and are made of stainless steel, and the space between the two plates is filled with a heat insulating material 14. The material of the heat insulating material is preferably ceramic wool. Preferably, the upper surface of the partition plate is carved with corrugated lines so as to guide the bitter water after the seawater desalination.
Preferably, the first-effect partition plate 13 and the second-effect partition plate are arranged obliquely. The partition plate in the distiller provided by the application has the characteristics of reducing and accelerating the flue gas below by oblique arrangement, so that the flue gas flows more smoothly; and simultaneously, the upper surface is combined with the carved lines so that the bitter water can be discharged more smoothly.
Preferably, flue gas heat exchange fins 12 are provided in the one-effect distiller for enhanced heat transfer.
Preferably, a steam deflector 22 is arranged in the cold end of the two-effect heat pipe of the two-effect distiller; the vapor baffle 22 is shown as corrugated interposed between the heat pipes. The steam deflector 22 is preferably made of a polyphenylene oxide material. The isomorphic corrugated steam guide plates are arranged to guide the steam to flow, so that the condensation and heat exchange of the steam are improved.
Preferably, the shell-and-tube heat exchanger 3 is vertically arranged above the fresh water bin 4, seawater is introduced into the shell, vapor distilled in the two-effect distiller is sucked into the tube, the vapor is liquefied in the tube and flows into the fresh water bin below, meanwhile, the seawater in the shell is preheated, and the preheated seawater enters the one-effect distiller and the two-effect distiller through the spraying device.
Preferably, the device further comprises a spray pipeline, wherein the inlet of the spray pipeline is connected with the seawater outlet of the shell-and-tube heat exchanger, and the outlet of the spray pipeline is connected with the one-effect distiller and the two-effect distiller. The seawater heated by the shell-and-tube heat exchanger enters the spray pipeline, so that the waste heat of the steam is fully utilized, and the desalination efficiency of the seawater is improved.
Preferably, the device also comprises a scale remover storage tank 5, wherein the scale remover storage tank is positioned above the first-effect distiller 1 and the second-effect distiller 2, stores scale remover inside and is connected with the spraying device. Preferably, the polyaspartic acid scale remover is stored in the interior and connected with a lower spray device, and the polyaspartic acid scale remover is sprayed when large-scale removal is needed. The chemical scale remover provided by the application is polyaspartic acid, is an environment-friendly scale inhibitor, and enables inorganic salt to be easily separated from the surface of an object through chelation dissolution and lattice distortion, so that the chemical scale remover has strong scale inhibition capability, is nontoxic and harmless, can be automatically degraded in the environment, and does not pollute the environment.
Preferably, the device comprises a Venturi ejector 7 which is arranged on a spray pipe of the one-effect distiller, and the air extraction end is connected with a fresh water bin. When seawater flows, negative pressure is pumped to the fresh water warehouse through the Venturi effect, and spray pressure is increased to make one-effect spraying more efficient.
The venturi tube ejector provided by the application is used in a seawater spraying pipeline, so that the negative pressure requirement in the device can be realized by flowing seawater, the requirement of the negative pressure distillation in the double-effect distiller is met, the use of a high-power vacuum pump is avoided, and the energy consumption is reduced; simultaneously, the pressure in the spraying pipeline can be increased by the pumped air, the flow speed of the sprayer in the first-effect distiller is larger, and the seawater atomization effect is better.
The air extraction end of the venturi tube is connected with the fresh water bin, when seawater flows through the venturi tube, part of air in the fresh water bin is extracted into the tube due to the venturi effect, and is injected into the one-effect distiller by the venturi tube, so that the fresh water bin is in a negative pressure state; because the fresh water bin, the shell-and-tube heat exchanger and the evaporation end of the double-effect distiller are mutually communicated through pipelines, the evaporation section of the double-effect distiller is in a negative pressure state, and distilled water vapor can be pumped into the shell-and-tube heat exchanger, so that the negative pressure requirement of the distillation device is met, and the water vapor can be smoothly led out for condensation.
Preferably, the evaporator comprises a foam-catching net which is arranged on a pipeline between the hot end of the first-effect distiller and the cold end of the second-effect distiller and on a pipeline between the hot end of the second-effect distiller and the shell-and-tube heat exchanger. Preferably a net-like structure made of polypropylene, for gas-liquid separation
Preferably, a flue gas filter is included, which is arranged in front of the inlet of the flue gas into the one-effect distiller. The stainless steel folding filter element is preferably composed of 304 stainless steel fiber sintered felt and a woven net.
Preferably, as shown in fig. 1, the seawater inlet pipe of the one-effect distiller is provided with a first valve. When the device works, firstly, the valves of the seawater inlet and outlet are used for controlling the spraying and water supplementing in the first-effect distiller, and when the seawater height in the first-effect distiller detected by the controller reaches a certain value, the spraying is stopped; when the evaporated bitter water in the one-effect distiller detected by the controller reaches a certain concentration, the bitter water drain valve of the one-effect distiller is opened, the bitter water is drained, and after the waste bitter water is drained, the valve at the bitter water outlet is closed, and water supplementing and spraying are performed again.
Preferably, as shown in fig. 2, the seawater inlet pipe of the double distiller is provided with a second valve. When the device works, firstly, the valve of the seawater inlet and outlet is used for controlling the spraying and water supplementing in the two-effect distiller, and when the seawater height in the two-effect distiller detected by the controller reaches a certain value, the spraying is stopped; when the evaporated bitter water in the two-effect distiller detected by the controller reaches a certain concentration, the bitter water drain valve of the two-effect distiller is opened, the bitter water is drained, and after the waste bitter water is drained completely, the valve at the bitter water outlet is closed, and water supplementing and spraying are performed again.
Through setting up automatic control drainage and spraying, can realize that sea water changes fresh water into in the maximum, realize the biggest result of utilization, reduce the scale deposit.
The spray header 7 is an atomizer.
Preferably, bitter water concentration detecting means is provided in the first-effect distiller and/or the second-effect distiller for detecting the concentration of bitter water, and the controller automatically controls the seawater discharge according to the detected bitter water concentration. If the measured bitter water concentration exceeds a certain value, the controller controls the bitter water outlet in the lower part of the distiller to open, and bitter water is discharged through the bitter water outlet.
Preferably, a water level detection device is arranged in the first-effect distiller and/or the second-effect distiller and is used for detecting the water level in the first-effect distiller and/or the second-effect distiller. When the water level is lower than certain data, the controller controls the opening of the first valve and/or the second valve to be increased, and the quantity of the entering spray water is increased.
Preferably, when the water level exceeds a certain data, for example, the water level is too high, the controller controls the opening degree of the first valve and/or the second valve to be reduced or closed, and reduces the amount of the entering shower water or stops the entering shower water.
Preferably, the shower head 7 has an annular circular tube structure, and a plurality of shower heads are distributed on the circular tube.
Through above-mentioned spraying structure and setting thereof, can realize intelligent operation, improved the efficiency of sea water desalination simultaneously.
Preferably, the device comprises a temperature equalizing device, wherein the temperature equalizing device is arranged on a pipeline for flue gas to enter the one-effect distiller.
As a modification, as shown in fig. 3, the flow guiding plate 52 extending from the inner wall 51 of the flue gas pipe to the center of the flue gas pipe is arranged in the flue gas pipe, the flow guiding plate 52 comprises a first straight line wall 521 and a second straight line wall 522 extending from the inner wall, wherein an acute angle formed by the first straight line wall 521 and the inner wall is smaller than an acute angle formed by the second straight line wall 522 and the inner wall, the first straight line wall 521 and the second curved wall 522 extend towards the flue gas flowing direction, and an intersection point 523 of the first straight line wall 521 and the second straight line wall 522 is positioned downstream of a joint of the first straight line wall 521 and the inner wall 51 and downstream of a joint of the second straight line wall 522 and the inner wall. The shape of the flow guiding plate 52 is a shape formed by the rotation of the first straight wall 521, the second straight wall 522 and the inner wall along the flue gas duct axis.
The temperature difference can occur in the layering due to different heat preservation at different positions and convection reasons in the transmission process of the flue gas, and particularly, under the condition of utilizing flue gas waste heat, the heat exchange in the distiller is uneven, and the heat exchange and the service life of a product are affected. According to the application, the flow guide plate is arranged in the flue gas pipeline, so that a part of flue gas is guided to the opposite direction along the flow of the flow guide plate and is fully mixed with the flue gas entering in the opposite direction, the temperature uniformity of the flue gas is realized, the further heat exchange requirement is realized, and the service life of a product is prolonged. And through setting up the second straight-line wall, the gradient of second straight-line wall is little moreover for the flue gas that gets over from opposite direction water conservancy diversion also can be along the upward direction motion of second straight-line wall direction, increases the buffering, reduces the flow resistance.
According to the application, the drainage plate is provided with the first straight-line wall and the second straight-line wall respectively, and by arranging the two straight-line walls, the disturbance effect of smoke is better, the area of the drainage plate contacting the inner wall is increased, and the stability is improved.
Preferably, the first straight wall 521 at the location of the intersection 523 forms an angle of 30-60, preferably 45, with the axis of the flue gas duct. By providing this angle, the fluid can be directed quickly to the opposite downstream location, and the flow resistance can be further reduced.
Preferably, as shown in fig. 3, multiple layers of drainage plates 52 are arranged on the inner wall of the flue gas pipeline along the flow direction of the flue gas, and the drainage plates of adjacent layers are distributed in a staggered manner. Through the staggered distribution of the drainage plates of adjacent rows, the flue gas can fully move to opposite positions in the flue gas pipeline, and the full and uniform mixing is ensured. For example, fig. 3 and 5 show that each layer of drainage plates is provided with one piece, and the total radian of the piece is 150-180 degrees. Of course, a plurality of drainage plates can be arranged on each layer, for example, three drainage plates are arranged on each layer in fig. 5, and the total radian is 150-180 degrees.
Preferably, the distance between the intersection point and the inner wall of the flue gas duct is 0.3-0.5 times, preferably 0.4 times, the diameter of the flue gas duct. By this arrangement the air is given less flow resistance on a well mixed basis.
Preferably, the length of the first straight wall is greater than the length of the second straight wall.
Preferably, the total radian of the circular arc connecting the drainage plates of the same layer with the inner wall is 150-180 degrees. By this parameter setting, a thorough mixing is ensured when the resistance requirement is met. For example, FIG. 2 shows that each layer of drainage plates is provided with one piece, and the total radian of the piece is 150-180 degrees. Of course, multiple drainage plates can be arranged on each layer, for example, two drainage plates can be arranged with the total radian of 150-180 degrees, or four drainage plates can be arranged with the total radian of 150-180 degrees.
Preferably, the A layer drainage plates are arranged in a plurality, the A layer drainage plates are arranged at intervals, the A layer drainage plates are arranged at equal intervals, the B layer is an adjacent row of the A layer, and the B layer drainage plates are arranged at intervals of the A layer when seen from the flowing direction. The positions of the drainage plates of the adjacent layers are complementary, so that the smoke can sufficiently move to the opposite positions in the smoke pipeline, and sufficient and uniform mixing is ensured. It should be noted that the layer a and the layer B are not specifically and explicitly specified, and A, B merely serves as a distinction between adjacent layers.
Preferably, a plurality of drainage plates are arranged on the inner wall of the flue gas pipeline along the flow direction of the flue gas, and the distribution density of the drainage plates is smaller and smaller along the flow direction of the flue gas. Because the mixing degree of the flue gas is better along with the continuous movement of the flue gas, the distribution density is required to be smaller and smaller to reduce the flow resistance, and the temperature equalizing effect achieves basically the same effect on the aspects of reducing the resistance and saving the material cost.
Preferably, the distribution density of the drainage plates is gradually increased along the flow direction of the flue gas. The effect is that the temperature equalizing effect reaches the basically same effect to the extent that the resistance is further reduced and the material cost is saved through a large number of numerical simulation and experimental research, and the research shows that the law accords with the law of the motion of the smoke.
Preferably, a plurality of drainage plates are arranged on the inner wall of the flue gas pipeline along the flow direction of the flue gas, and the size of the drainage plates is smaller and smaller along the flow direction of the flue gas. Because the mixing degree of the flue gas is better and better along with the continuous movement of the flue gas, the size is required to be smaller and smaller to reduce the flow resistance, and the temperature equalizing effect achieves basically the same effect on the aspects of reducing the resistance and saving the material cost.
Preferably, a plurality of drainage plates are arranged on the inner wall of the flue gas pipeline along the flow direction of the flue gas, and the size of the drainage plates is gradually increased along the flow direction of the flue gas. The effect is that the temperature equalizing effect reaches the basically same effect to the extent that the resistance is further reduced and the material cost is saved through a large number of numerical simulation and experimental research, and the research shows that the law accords with the law of the motion of the smoke.
Through a large number of numerical simulation and experimental researches, the angle and the size of the drainage plate have great influence on heat exchange and uniform mixing, the included angle between the drainage plate and the inner wall is smaller, the mixing effect is poor, the size of the drainage plate is too large, the flowing resistance is influenced, the included angle is larger, the stirring fluid effect is poor, the resistance is large, the mixing effect is poor, the interval between the drainage plates is too large, the turbulence effect is poor, and the movement resistance is increased due to the too small interval.
Preferably, the length L2 of the first straight wall, the length L1 of the second straight wall, the acute angle between the first line and the inner wall is A2, the acute angle between the second line and the inner wall is A1, the distance S between adjacent drainage plate structures along the flow direction of the flue gas, that is, the distance between the center points of the adjacent drainage plates and the inner wall, the center point is the midpoint of the connecting line of the connecting points of the first straight wall, the second straight wall and the inner wall, and the following requirements are satisfied:
n=a-b Ln (M), where n= (l1+l2)/S, m=sin (A2)/sin (A1); ln is a logarithmic function that is a function of the number of pairs,
0.3125<a<0.3130，0.1268<b<0.1272；
preferably, 0.25< M <0.75,0.34< N <0.44,45< A1<75 °,15< A2<65 °,350< S <500mm,70< L2<130mm,30< L1<90mm.
The optimal design requirements of the drainage plate structure can be met by the above-mentioned various types. The above structural optimization formula is a main improvement point of the present application, is the most effective optimization formula which is researched by a large number of numerical simulations and experiments, and is not common knowledge in the art.
Further preferably, a=0.3128 and b=0.1270.
In data simulation and experiments, the interval between the drainage plates is found to be larger than a certain distance, otherwise, fluid is led to the opposite direction through the last drainage plate, but if the interval between the drainage plates is too small, flue gas flows across the opposite direction and is not fully filled in the whole pipeline, at the moment, the drainage plates are arranged to play a role in mixing, the drainage plates only play a role in a baffle plate, do not conduct mixing, and only can flow resistance be increased. Therefore, through a great deal of researches, the application provides a design scheme of the minimum spacing of the drainage plates, and has certain guiding significance for the design of the drainage plates.
The intersection point 523 is a perpendicular point on the inner wall, a line formed by the intersection point and the perpendicular point is a third line, the distance between the connection point of the first straight line wall and the inner wall and the perpendicular point is H, the inner pipe diameter of the flue gas pipeline is R, and the distance S is designed in the following way:
S1>＝a*H+b*((H) 2 +R 2 ) (1/2) ；
wherein the method comprises the steps of
Preferably, a=3.2, c=1.557;
according to the application, through a large number of experiments and numerical simulation, the minimum design distance of the drainage plate is obtained, and the resistance is reduced through the design distance, so that the drainage plate can be fully mixed.
As shown in fig. 2, the two-effect distiller 2 and the shell-and-tube heat exchanger 3 are overlapped on the fresh water bin 4, the one-effect distiller 1 is discharged on the side of the two-effect distiller, a pipeline above the shell-and-tube heat exchanger 3 is divided into two paths to be respectively introduced into a distillation chamber and connected with an atomization sprayer in the distillation chamber, a venturi sprayer is additionally arranged on the one-effect spraying pipeline, an air extraction end is connected with the fresh water bin, seawater is pumped into a shell part of the shell-and-tube heat exchanger 3 by a centrifugal pump after being filtered, and then sprayed into the distillation chamber by the pipeline. The flue gas is led out by a bypass of a main engine exhaust pipeline, filtered and blown into the lower part of the one-effect distiller 1 by a blower, and then is discharged from the other end. The vapor evaporated from the first-effect distiller 1 is introduced into the cold end of the lower part of the second-effect distiller 2 through a glass fiber reinforced plastic pipeline, and a foam-catching net is additionally arranged at the part of the pipeline close to the first-effect distiller so as to remove atomized seawater mixed in the vapor; the same structure and the same function are also arranged on the pipeline connecting the double-effect distiller 2 and the shell-and-tube heat exchanger 3. The bottom ends of the two distiller separating plates in the inclined direction are connected with pipelines and finally gathered into one path for discharging bitter water.
When the device works, the PID control system 6 controls the flow of the flue gas and the spraying amount of the seawater; when flue gas is introduced into the hot end of the first effect distiller 1, the heat of the flue gas is transferred to the upper hot end through the high-temperature heat pipe 11, sprayed cold sea water is distilled, the vapor distilled by the first effect is led into the cold end of the second effect distiller 2, on one hand, the vapor is liquefied into fresh water when meeting cold and flows into the lower fresh water bin 4, on the other hand, the liquefied latent heat of the vapor is transferred to the upper hot end of the heat pipe through the second effect heat pipe 21, the second effect sprayed sea water is distilled, the vapor distilled by the second effect is introduced into the shell-and-tube heat exchanger 3 to exchange heat with the cold sea water, and the fresh water flows into the lower fresh water bin 4 when preheating the sea water, so that the sources of the fresh water are divided into two parts: part of the water vapor is liquefied from the cold end of the heat pipe in the second effect distiller, and the other part of the water vapor is liquefied from the fresh water in the shell-and-tube heat exchanger. The residual bitter water after distillation is led out from the inclined lower end of the partition plate, and the two paths are converged and discharged outwards.
The tank body of the first-effect distiller 1 is square, round corners are led around the tank body, the tank body is made of single-layer duplex stainless steel, and composite silicate heat-insulating paint is coated on the outer part of the tank body; the upper sealing cover can be disassembled, and the periphery is sealed by eight bolts; the top of the tank body is provided with a scale inhibitor storage tank, polyaspartic acid scale inhibitor is stored in the tank body, and the lower part of the tank body is connected with a sprayer in the distiller through a pipeline; atomizing sprayers are uniformly distributed on the periphery of the scale inhibitor sprayer to spray seawater; a high-temperature heat pipe array is vertically arranged in the distiller; the partition plates are obliquely arranged, and the surfaces of the upper half parts are carved with diversion lines so as to lead out bitter water rapidly; glass wool is filled between the two layers of partition plates for heat insulation. Transverse fins are welded on the lower part of the high-temperature heat pipe.
The whole structure of the two-effect distiller 2 is similar to that of a one-effect distiller, but the selection of the heat pipe and the selection of the hot end fins are different; the heat pipe of the two-effect distiller adopts a traditional heat pipe; corrugated guide plates made of polyphenyl ether materials are vertically arranged at the lower part of the heat pipe and are inserted between the heat pipe arrays so as to provide turbulence and enable steam and the heat pipe to exchange heat efficiently and flow into a fresh water bin below after liquefaction.
The inner part of the shell-and-tube heat exchanger 3 is provided with a tube body and a shell, wherein the tube body and the shell are mutually independent spaces, the tube body is a straight tube and is communicated up and down, and steam in the two-effect distiller is introduced from top to bottom into the tube body; the shell is internally provided with spoilers which are alternately arranged left and right, and sea water is introduced from bottom to top; the heat exchange is carried out between the steam and the seawater, the steam is liquefied into fresh water, and the seawater is preheated in advance.
The fresh water bin 4 is made of 304 stainless steel, is arranged below the two-effect distiller and the shell-and-tube heat exchanger, is simultaneously provided with holes on the side surface and connected with the suction end of a venturi jet device on a seawater spray pipeline through a hose, and can pump the fresh water bin into negative pressure when seawater flows, so that distilled water vapor flows and is liquefied; meanwhile, due to the communication among the pipelines, the negative pressure can also reduce the pressure at the distillation end of the double-effect distiller and lower the boiling point of seawater.
The device is divided into two parts for controlling the scaling of the seawater, and the device determines whether to spray and remove the scale according to the scaling condition by sensor data in normal operation, and mainly ensures that sodium chloride adhered to a heat pipe during distillation is discharged along with the seawater through dissolution by increasing the spraying quantity of the seawater and opening a bitter water outlet; when the sensor detects that the surface of the heat pipe is provided with excessive inorganic salt with smaller solubility, such as magnesium sulfate, calcium sulfate and the like, the sensor can automatically spray the scale inhibitor to carry out chemical descaling, and simultaneously, the sensor is matched with seawater with large spraying quantity to wash out scale.
Preferably, the heat exchanger further comprises a scale remover storage tank, wherein the scale remover storage tank is positioned above the heat exchanger, is internally stored with the scale remover and is connected with the spraying device through a valve.
Preferably, the descaling system is controlled by a control system, and a diffuse reflection optical fiber sensor is arranged in the distiller. The control flow is as follows: when the device is in normal operation, the diffuse reflection optical fiber sensor senses the scaling condition on the heat pipe, when the scaling quantity is too large, the spraying quantity of seawater is increased, meanwhile, the bitter water discharging electromagnetic valve is opened, the time is regularly flushed by the timer, and soluble salts such as sodium chloride and the like on the heat pipe are removed by a dissolution method; when the sensor detects that the scaling amount is still at a higher value after a plurality of flushing, the polyaspartic acid scale inhibitor is sprayed so as to remove salts with smaller solubility, such as magnesium sulfate, calcium sulfate and the like, through the chelation dissolution and lattice distortion principles.
Preferably, the control system consists of a sensor, a microprocessor and a PID module; each sensor transmits data such as flue gas temperature, flue gas flow, sea water temperature, sea water flow, evaporating chamber temperature and the like to the microcontroller, the microcontroller accurately calculates the flow of required flue gas and the spraying amount of sea water according to an algorithm compiled in the microcontroller, the data is fed back to the PID module, and the accurate control of the flue gas flow and the sea water spraying amount is realized through a proportional-integral-derivative closed-loop control system formed by the PID module, so that the device can still produce fresh water according to the expected water yield under a complex external environment, and the fresh water can be produced efficiently and stably.
Heat pipe evaporation end and condensationThe heat exchange coefficients of the ends are k respectively 1 ,k 2 The method comprises the steps of carrying out a first treatment on the surface of the The heat exchange areas of the evaporating end and the condensing end of the heat pipe are respectively A 1 ,A 2 The method comprises the steps of carrying out a first treatment on the surface of the According to the calculation formula of flat wall heat transfer coefficient and rib wall heat transfer coefficient The heat exchange coefficient k of the evaporating end and the condensing end of the heat pipe is obtained by substituting the physical parameters of the material and the cold and hot fluid and the corresponding parameters calculated by combining the heat transfer characteristic number into the formula 1 ,k 2 The method comprises the steps of carrying out a first treatment on the surface of the The temperature difference between the flue gas and the seawater obtained by the temperature sensor is delta t 1 ,Δt 2 The method comprises the steps of carrying out a first treatment on the surface of the Thus, the heat flow rate Q of the flue gas can be calculated 1 ＝k 1 A 1 Δt 1 The method comprises the steps of carrying out a first treatment on the surface of the Sea water absorbs heat Q 2 ＝k 2 A 2 Δt 2 The method comprises the steps of carrying out a first treatment on the surface of the Then determining smoke amount +.>Seawater spraying quantity->
The above embodiments are provided to illustrate the technical concept and features of the present application and are intended to enable those skilled in the art to understand the content of the present application and implement the same, and are not intended to limit the scope of the present application. All equivalent changes or modifications made in accordance with the spirit of the present application should be construed to be included in the scope of the present application.
Claims (5)
1. The sea water desalinating device based on ship waste gas waste heat is characterized by comprising an effective distiller, a two-effective distiller, a shell-and-tube heat exchanger and a fresh water bin, wherein the effective distiller is connected with the two-effective distiller, the two-effective distiller is connected with the shell-and-tube heat exchanger, the fresh water bin is arranged at the lower parts of the two-effective distiller and the shell-and-tube heat exchanger, the effective distiller is an intelligent descaling heat exchanger, the heat exchanger comprises a shell, a heat pipe and a division plate, the heat pipe is arranged in the shell, the division plate divides the heat pipe into a hot end positioned at the upper part and a cold end positioned at the lower part, and is characterized in that flue gas enters the lower part of the division plate, sea water is sprayed above the division plate, the heat exchanger further comprises a descaling agent storage tank, the descaling agent storage tank is positioned above the heat exchanger, is internally stored with a descaling agent and is connected with a spraying device through a valve, a diffuse reflection optical fiber sensor is arranged in the heat exchanger, when the device normally operates, the diffuse reflection optical fiber sensor senses the scaling condition, when the scaling condition is detected, the scaling condition is excessive, the heat pipe is increased, the spraying quantity is carried out, and the bitter water is simultaneously, and the valve is opened; when the sensor detects that the scaling amount is still at a higher value after a plurality of times of flushing, the controller controls the valve of the descaling agent storage tank to be opened, and the descaling agent is sprayed onto the heat exchange tube through the spraying device; the flue gas is introduced into the cold end of the first-effect distiller, the flue gas heat is transferred to the upper hot end through the cold end of the high-temperature heat pipe, sprayed cold sea water is distilled, vapor distilled by the first-effect distiller is led into the cold end of the second-effect distiller, on one hand, the vapor is liquefied into fresh water when meeting cold and flows into a fresh water bin below, on the other hand, the liquefied latent heat of the vapor is transferred to the hot end above the second-effect heat pipe through the second-effect heat pipe, the sprayed sea water of the second-effect distiller is distilled, the vapor distilled by the second-effect distiller is introduced into a shell-and-tube heat exchanger for heat exchange with the cold sea water, and the vapor is liquefied into fresh water when preheating the sea water and flows into the fresh water bin below; the seawater desalination device comprises a temperature equalization device, the temperature equalization device is arranged on a pipeline for flue gas to enter the one-effect distiller, the temperature equalization device comprises a drainage plate extending from the inner wall of the flue gas pipeline to the center of the flue gas pipeline, the drainage plate comprises a first curved wall and a second curved wall, the acute angle formed by the tangent line of the junction of the first curved wall and the inner wall is smaller than the acute angle formed by the tangent line of the junction of the second curved wall and the inner wall, the first curved wall and the second curved wall are curved and extend towards the flue gas flowing direction, the curved direction is also towards the flue gas flowing direction, the intersection point of the first curved wall and the second curved wall is positioned downstream of the junction of the first curved wall and the inner wall, and meanwhile, the intersection point of the first curved wall and the second curved wall is positioned downstream of the junction of the second curved wall and the inner wall; the shape of the drainage plate is formed by rotating a first curved wall, a second curved wall and an inner wall along the axis of the flue gas pipeline; along the flow direction of flue gas, flue gas pipeline inner wall sets up a plurality of drainage plates, along the flow direction of flue gas, the distribution density of drainage plate is less and less.
2. The seawater desalination plant of claim 1, wherein the detergent is a polyaspartic acid detergent and is connected to the lower spray means.
3. The desalination apparatus of claim 1, wherein the heat pipe is periodically flushed a plurality of times by increasing the spray level of seawater when the detected fouling level is excessive.
4. The seawater desalination plant of claim 1, wherein the shell-and-tube heat exchanger is vertically disposed above the fresh water tank, seawater is introduced into the shell, vapor distilled in the two-effect distiller is sucked into the tube, the vapor is liquefied in the tube and flows into the fresh water tank below, the seawater in the shell is preheated at the same time, and the preheated seawater enters the one-effect distiller and the two-effect distiller through the spraying device.
5. The desalination apparatus of claim 1, further comprising a spray line, an inlet of the spray line connecting the seawater outlet of the shell and tube heat exchanger, and an outlet of the spray line connecting the first and second effect distillers.
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| CN2280708Y (en) * | 1996-12-31 | 1998-05-06 | 江苏理工大学 | Heat-pipe type sea-water desalinating device |
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| CN110655133A (en) * | 2018-10-29 | 2020-01-07 | 山东大学 | Seawater concentration intelligent control method of circulating spray heat exchange system |
| CN111174633A (en) * | 2020-01-13 | 2020-05-19 | 刘倩倩 | Self-descaling electric water heater |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2280708Y (en) * | 1996-12-31 | 1998-05-06 | 江苏理工大学 | Heat-pipe type sea-water desalinating device |
| CN101948148A (en) * | 2010-10-22 | 2011-01-19 | 河北宏润重工集团有限公司 | Energy-saving low-temperature multiple-effect seawater desalting device |
| CN106610151A (en) * | 2015-10-22 | 2017-05-03 | 丹佛斯微通道换热器（嘉兴）有限公司 | Heat exchanger |
| CN106115825A (en) * | 2016-08-19 | 2016-11-16 | 北京今大禹环境技术股份有限公司 | A kind of low temperature multiple-effect distillation seawater desalination system |
| CN108190988A (en) * | 2017-12-29 | 2018-06-22 | 常州思宇知识产权运营有限公司 | A kind of heat-pipe type sea-water desalinating using fume afterheat |
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