CN114477345A - Loop heat pipe and heat control system thereof - Google Patents
Loop heat pipe and heat control system thereof Download PDFInfo
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- CN114477345A CN114477345A CN202011271049.2A CN202011271049A CN114477345A CN 114477345 A CN114477345 A CN 114477345A CN 202011271049 A CN202011271049 A CN 202011271049A CN 114477345 A CN114477345 A CN 114477345A
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- effect
- distiller
- seawater
- effect distiller
- fresh water
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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
Abstract
The utility model provides a sea water desalination device of ejector waste gas waste heat, a serial communication port, the device is including an effect distiller, two effect distiller, shell and tube type heat exchanger and fresh water storehouse, two effect distiller is connected to an effect distiller, and two effect distiller connects shell and tube type heat exchanger, fresh water storehouse sets up the lower part at two effect distiller and shell and tube type heat exchanger, the device still includes the venturi ejector, and it is installed on the shower pipeline of an effect distiller, and fresh water storehouse is connected to the end of bleeding. The venturi tube ejector provided by the invention 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 negative pressure distillation in a two-effect distiller is met, the use of a high-power vacuum pump is avoided, and the energy consumption is reduced; meanwhile, the pressure intensity in the spraying pipeline is increased by the extracted air, the flow velocity of a sprayer in the single-effect distiller is larger, and the seawater atomization effect is better.
Description
Technical Field
The invention belongs to the field of seawater desalination, and particularly provides a seawater desalination device taking flue gas as a desalination heat source under the using condition of a ship
Background
At present, the seawater 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 enables the overall heat utilization rate to be higher by recycling steam heat, but the device is huge due to the existence of the multi-effect evaporator, and is often built on coastal lands to produce fresh water; the multi-stage flash evaporation method comprises the steps of firstly heating seawater, then introducing the seawater into a distillation tank with gradually reduced pressure intensity, and carrying out gradual distillation by utilizing the characteristic that the boiling point of water is reduced along with the reduction of the pressure intensity; the RO method is to pressurize seawater by the semi-permeability of the semi-permeable membrane to water molecules, and to make the water molecules penetrate through the semi-permeable membrane by utilizing the pressure difference principle, so as to complete the separation of water and salt.
The main engine of the ship is a diesel engine, only 45-50% of heat generated by burning fuel oil in the diesel engine is converted into mechanical energy, about 50% of energy released by burning is dissipated as waste heat, 25-30% of heat is taken away by waste gas, and a large amount of waste heat is directly discharged into the air, so that energy waste and environmental pollution are caused.
Because a large amount of low-grade heat energy in flue gas discharged by a ship main engine is not utilized, and a thermal method is used as a direct heat source for providing desalination energy in the device based on the seawater desalination principle, the idea of taking ship waste gas as a desalination heat source is brought forward, and the advantages and the characteristics of a multi-effect distillation method and a multi-stage flash evaporation method are combined to design the device.
Disclosure of Invention
The invention aims to provide a heat source for a seawater desalination device based on a multi-effect distillation method by utilizing waste heat in flue gas discharged by ships, and produce fresh water on ships in an efficient and energy-saving manner.
The technical scheme of the invention is as follows: the utility model provides a sea water desalination device of ejector waste gas waste heat, a serial communication port, the device is including an effect distiller, two effect distiller, shell and tube type heat exchanger and fresh water storehouse, two effect distiller is connected to an effect distiller, and two effect distiller connects shell and tube type heat exchanger, fresh water storehouse sets up the lower part at two effect distiller and shell and tube type heat exchanger, the device still includes the venturi ejector, and it is installed on the shower pipeline of an effect distiller, and fresh water storehouse is connected to the end of bleeding.
Preferably, the fresh water bin is arranged below the double-effect distiller and the shell-and-tube heat exchanger, and the side opening of the fresh water bin is connected with the suction end of the venturi ejector on the seawater spraying pipeline through a hose.
Preferably, the flue gas is filtered, blown into the lower part of the single-effect distiller by a blower and then discharged from the other end.
Preferably, a first-effect heat pipe and a first-effect partition plate are arranged in the first-effect distiller, the first-effect partition plate divides the first-effect heat pipe into a hot end positioned at the upper part and a cold end positioned at the lower part, a second-effect heat pipe and a second-effect partition plate are arranged in the second-effect distiller, the second-effect partition plate divides the second-effect heat pipe into a hot end positioned at the upper part and a cold end positioned at the lower part, the flue gas is introduced into the cold end of the first-effect distiller, the heat of the flue gas is transferred to the hot end at the upper part through the cold end of the high-temperature heat pipe to distill the cold seawater sprayed down, the steam distilled out by the first-effect distiller is introduced into the cold end of the second-effect distiller, the steam on one hand is liquefied into fresh water to flow into the fresh water bin at the lower part, the latent heat of liquefaction of the steam on the other hand is transferred to the hot end at the upper part of the second-effect heat pipe through the second-effect heat pipe to distill the spray seawater of the second-effect distiller, and the steam distilled out by the second-effect distiller is introduced into a shell-and-tube heat exchanger, exchanging heat with cold seawater in a shell-and-tube heat exchanger, and liquefying the water vapor into fresh water while preheating the seawater to flow into a lower fresh water bin.
Preferably, the first-effect separation plate and the second-effect separation plate have two layers and are made of stainless steel, and the space between the two layers is filled with a heat insulation material.
Preferably, a steam guide plate is arranged in the cold end of the double-effect heat pipe of the double-effect distiller; the steam guide plate is inserted between the heat pipes in a corrugated shape.
Preferably, the shell-and-tube heat exchanger is vertically arranged above the fresh water bin, seawater is introduced into the shell, steam distilled out of the double-effect distiller is absorbed into the tube body, the steam is liquefied in the tube body and flows into the fresh water bin below, meanwhile, the seawater in the shell is preheated, and the preheated seawater enters the primary-effect distiller and the double-effect distiller through the spraying device.
Preferably, the seawater desalination device further comprises a spraying pipeline, an inlet of the spraying pipeline is connected with a seawater outlet of the shell-and-tube heat exchanger, and an outlet of the spraying pipeline is connected with the first-effect distiller and the second-effect distiller.
Preferably, the device also comprises a descaling agent storage tank which is positioned above the single-effect distiller (1) and the double-effect distiller (2), stores descaling agent inside and is connected with the spraying device.
Preferably, the system comprises a Venturi ejector which is arranged on a spraying pipeline of the single-effect distiller, and an air exhaust end of the Venturi ejector is connected with a fresh water bin.
Preferably, the system 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 a connecting pipeline between the hot end of the second-effect distiller and the shell-and-tube heat exchanger.
Preferably, the flue gas filter is arranged at the front section of an inlet of the flue gas into the single-effect distiller.
Preferably, the system comprises a temperature equalizing device, wherein the temperature equalizing device is arranged on a pipeline for the flue gas to enter the single-effect distiller.
The invention has the beneficial effects that:
1. the venturi tube ejector provided by the invention 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 negative pressure distillation in a double-effect distiller is met, the use of a high-power vacuum pump is avoided, and the energy consumption is reduced; meanwhile, the pressure intensity in the spraying pipeline is increased by the extracted air, the flow velocity of a sprayer in the single-effect distiller is larger, and the seawater atomization effect is better.
2. According to the double-effect reduced pressure distillation device integrating multiple-effect distillation and a multi-stage flash evaporation method, the seawater is distilled by absorbing heat of flue gas in the first effect, the distilled water vapor is led into the double-effect distiller, and on one hand, the water vapor releases latent heat of liquefaction to the heat pipe and on the other hand is liquefied into fresh water; the water vapor distilled from the two-effect distiller exchanges heat with the shell-and-tube heat exchanger, and releases latent heat of liquefaction to untreated seawater while liquefying into fresh water, so as to play a role in 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 conducted to the water vapor, and greatly improves the utilization efficiency of the heat energy through the complementary relation of liquefaction, heat release, evaporation and heat absorption.
3. According to the distiller provided by the invention, the partition plates are obliquely arranged, so that the flue gas below has the characteristic of diameter-changing acceleration, and the flue gas flows more smoothly; simultaneously, the discharge of the bitter water is smoother by combining the engraved lines on the upper surface.
4. The chemical descaling agent provided by the invention is polyaspartic acid, which is an environment-friendly scale inhibitor, inorganic salt is easy to separate from the surface of an object through chelating dissolution and lattice distortion, and the scale inhibitor has strong scale inhibition capability, is non-toxic and harmless, can be automatically degraded in the environment, and cannot pollute the environment.
5. The invention provides a novel temperature equalizing device, wherein a flow guide plate is arranged in a flue gas pipe, so that a part of gas flows along the flow guide plate and is guided to the opposite direction, and the gas is fully mixed with the gas entering in the opposite direction, so that the temperature of the gas is uniform, the requirement of further heat exchange is met, and the service life of a product is prolonged.
Drawings
FIG. 1 is a schematic view of the device of the present invention
FIG. 2 is an isometric view of a three-dimensional model of the present invention
FIG. 3 is an axial sectional view of a flue gas duct of the present invention with flow-diverting plates;
fig. 4 is a schematic diagram of the size of the flue gas duct installation draft plate of the present invention.
FIG. 5 is a perspective view of 1 drainage plate per layer.
FIG. 6 is a perspective view of 3 drainage plates per layer.
Detailed Description
The technical solution in the embodiment of the present invention will be described in addition with the accompanying drawings in the embodiment of the present invention.
A seawater desalination device based on ship waste gas waste heat is disclosed, as 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-and-tube 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 partition plate 13 are arranged in the first-effect distiller 1, the first-effect heat pipe 11 is divided into a hot end at the upper part and a cold end at the lower part by the first-effect partition plate 13, a second-effect heat pipe 21 and a second-effect partition plate are arranged in the second-effect distiller 2, the second-effect partition plate divides the second-effect heat pipe into a hot end at the upper part and a cold end at the lower part, the flue gas is introduced into the cold end of the first-effect distiller 1, and the heat of the flue gas is transferred to the hot end at the upper part by the cold end of the high-effect heat pipe 11, the sprayed cold seawater is distilled, the water vapor distilled by the first-effect distiller 1 is led into the cold end of the second-effect distiller 2, the water vapor on one hand is liquefied into fresh water to flow into a lower fresh water bin 4 when meeting cold, the latent heat of liquefaction of the water vapor on the other hand is transferred to the hot end above the second-effect heat pipe 21 through the second-effect heat pipe 21, the sprayed seawater of the second-effect distiller 2 is distilled, the water vapor distilled by the second-effect distiller 2 enters a shell-and-tube heat exchanger 3 to exchange heat with the cold seawater in the shell-and-tube heat exchanger 3, and the water vapor is liquefied into fresh water to flow into the lower fresh water bin 4 when preheating the seawater.
According to the double-effect reduced pressure distillation device integrating multiple-effect distillation and a multi-stage flash evaporation method, the seawater is distilled by absorbing heat of flue gas in the first effect, the distilled water vapor is led into the double-effect distiller, and on one hand, the water vapor releases latent heat of liquefaction to the heat pipe and on the other hand is liquefied into fresh water; the water vapor distilled from the two-effect distiller exchanges heat with the shell-and-tube heat exchanger, and releases latent heat of liquefaction to untreated seawater while liquefying into fresh water, so as to play a role in 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 conducted to the water vapor, and greatly improves the utilization efficiency of the heat energy through the complementary relation of liquefaction, heat release, evaporation and heat absorption.
Preferably, the first-effect separator plate 13 and the second-effect separator 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 provided with corrugated lines so as to guide the bitter water after seawater desalination.
Preferably, the first-effect separation plate 13 and the second-effect separation plate are arranged obliquely. According to the distiller provided by the invention, the partition plates are obliquely arranged, so that the flue gas below has the characteristic of diameter-changing acceleration, and the flue gas flows more smoothly; simultaneously, the discharge of the bitter water is smoother by combining the engraved lines on the upper surface.
Preferably, the flue gas heat exchange fins 12 are arranged in the single-effect distiller and used for enhancing heat transfer.
Preferably, a steam guide plate 22 is arranged in the cold end of the double-effect heat pipe of the double-effect distiller; the vapor deflector 22 is corrugated to penetrate between the heat pipes. The vapor deflector 22 is preferably made of a polyphenylene ether material. The isomorphism sets up corrugate steam guide plate, and the guide steam flows, improves the condensation and the heat transfer of steam.
Preferably, the shell-and-tube heat exchanger 3 is vertically arranged above the fresh water bin 4, seawater is introduced into the shell, water vapor distilled out of the double-effect distiller is absorbed into the tube body, the water vapor is liquefied in the tube body and flows into the fresh water bin below, meanwhile, the seawater in the shell is preheated, and the preheated seawater enters the primary-effect distiller and the double-effect distiller through the spraying device.
Preferably, the seawater desalination device further comprises a spraying pipeline, an inlet of the spraying pipeline is connected with a seawater outlet of the shell-and-tube heat exchanger, and an outlet of the spraying pipeline is connected with the first-effect distiller and the second-effect distiller. Seawater heated by the shell-and-tube heat exchanger enters the spraying pipeline, waste heat of steam is fully utilized, and seawater desalination efficiency is improved.
Preferably, the descaling device further comprises a descaling agent storage tank 5, wherein the descaling agent storage tank is positioned above the first-effect distiller 1 and the second-effect distiller 2, stores descaling agent inside, and is connected with the spraying device. Preferably, the polyaspartic acid scale remover is stored inside and is connected with a lower spraying device, and the polyaspartic acid scale remover is sprayed when large-scale removal is needed. The chemical descaling agent provided by the invention is polyaspartic acid, which is an environment-friendly scale inhibitor, inorganic salt is easy to separate from the surface of an object through chelating dissolution and lattice distortion, and the scale inhibitor has strong scale inhibition capability, is non-toxic and harmless, can be automatically degraded in the environment, and cannot pollute the environment.
Preferably, the device comprises a Venturi ejector 7 which is arranged on a spray pipeline of the single-effect distiller, and an air exhaust end of the Venturi ejector is connected with a fresh water bin. When the sea water flows, negative pressure is pumped out for the fresh water bin through the venturi effect on the one hand, and spray pressure is increased on the other hand, so that one-effect spraying is more efficient.
The venturi tube ejector provided by the invention 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 negative pressure distillation in a two-effect distiller is met, the use of a high-power vacuum pump is avoided, and the energy consumption is reduced; meanwhile, the pressure intensity in the spraying pipeline is increased by the extracted air, the flow velocity of a sprayer in the single-effect distiller is larger, and the seawater atomization effect is better.
The air exhaust end of the venturi tube is connected with the fresh water bin, when seawater flows through the venturi tube, part of air of the fresh water bin is pumped 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 the pipeline, the evaporation section of the double-effect distiller is also 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 system 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 a connecting pipeline between the hot end of the second-effect distiller and the shell-and-tube heat exchanger. Preferably a net structure of polypropylene, for gas-liquid separation
Preferably, the flue gas filter is arranged at the front section of an inlet of the flue gas into the single-effect distiller. Preferably a stainless steel pleated filter element comprised of a 304 stainless steel fiber sintered felt and a woven mesh.
Preferably, as shown in fig. 1, the seawater inlet pipe of the single-effect distiller is provided with a first valve. When the device works, firstly, the valve control of the seawater inlet and outlet is used for spraying and supplementing water in the primary effect distiller, and when the seawater height in the primary effect distiller detected by the controller reaches a certain height, the spraying is stopped; when the bitter water evaporated in the first-effect distiller detected by the controller reaches a certain concentration, the bitter water drainage valve of the first-effect distiller is opened, the bitter water is drained, after the waste bitter water is drained, the valve at the bitter water outlet is closed, and water replenishing and spraying are carried out again.
Preferably, as shown in fig. 2, the seawater inlet pipe of the double-effect distiller is provided with a second valve. When the device works, firstly, the valve control of the seawater inlet and outlet is used for spraying and supplementing water in the double-effect distiller, and when the seawater height in the double-effect distiller detected by the controller reaches a certain height, the spraying is stopped; when the bitter water evaporated in the double-effect distiller detected by the controller reaches a certain concentration, the bitter water drainage valve of the double-effect distiller is opened, the bitter water is drained, after the waste bitter water is drained, the valve at the bitter water outlet is closed, and water replenishing and spraying are carried out again.
Through setting up automatic control drainage and spraying, can realize that the sea water furthest converts into fresh water, realizes the biggest utilization effect, reduces the scale deposit.
The spray head 7 is an atomizing spray head.
Preferably, a bitter water concentration detection device is arranged in the first-effect distiller and/or the second-effect distiller and used 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 at the lower part of the distiller to be opened, and the 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 height 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 amount of the entering spray water is increased.
Preferably, when the water level exceeds a certain value, for example, the water level is too high, the controller controls the opening of the first valve and/or the second valve to be reduced or closed, reduces the amount of shower water to be introduced, or stops the introduction of shower water.
Preferably, the shower head 7 is an annular circular tube structure, and a plurality of shower heads are distributed on the circular tube.
Through the spraying structure and the arrangement thereof, intelligent operation can be realized, and the efficiency of seawater desalination is improved.
Preferably, the system comprises a temperature equalizing device, and the temperature equalizing device is arranged on a pipeline for the flue gas to enter the single-effect distiller.
As a modification, the temperature equalizing device is as shown in FIG. 3, a flow guiding plate 52 extending from the inner wall 51 of the flue gas duct to the center of the flue gas duct is arranged in the flue gas duct, and the flow guiding plate 52 comprises a first curved wall 521 and a second curved wall 522 extending from the inner wall, wherein the acute angle formed by the tangent line at the connection position of the first curved wall 521 and the inner wall 51 and the inner wall is smaller than the acute angle formed by the tangent line at the connection position of the second curved wall 522 and the inner wall, the first curved wall 521 and the second curved wall 522 extend in a curved manner towards the flow direction of flue gas, the curved direction is also towards the flow direction of flue gas, and the intersection point 523 of the first curved wall 521 and the second curved wall 522 is located downstream of the connection position of the first curved wall 521 and the inner wall 51 and downstream of the connection position of the second curved wall 522 and the inner wall. The shape of the flow guide plate 52 is the shape formed by the first 521 and second 522 curved walls and the inner wall rotated along the axis of the flue gas duct.
The flue gas can lead to the layering to appear the difference in temperature because different positions keep warm different and convection reason in the transmission course, especially to many mouthfuls of input flue gas, utilizes under the flue gas waste heat condition, leads to heat transfer inhomogeneous in the distiller, influences the heat transfer and the life-span of product. The invention provides a flue gas heat exchanger, which is characterized in that the flow guide plate is arranged in the flue gas pipeline, so that a part of flue gas flows along the flow guide plate and is guided to the opposite direction, and the flue gas is fully mixed with the flue gas entering from the opposite direction, thereby realizing uniform temperature of the flue gas, realizing the requirement of further heat exchange and prolonging the service life of products.
According to the invention, the drainage plate is respectively provided with the first bending wall and the second bending wall, and the two bending walls are arranged, so that the disturbance effect of smoke is better, the area of the drainage plate contacting the inner wall is increased, and the stability is improved. And through setting up the second crooked wall for flue gas that the opposite direction water conservancy diversion was come also can be along the crooked direction motion of second crooked wall direction, increases the buffering, reduces flow resistance.
Preferably, the first curved wall 521 and the second curved wall 522 are arcs, wherein the diameter of the arc of the first curved wall 521 is smaller than the diameter of the arc of the second curved wall 522.
According to the invention, the first wall and the second wall are arc-shaped, so that the smoke flowing resistance is smaller, and the smoke is easy to flow to the opposite side for mixing.
Preferably, the tangent to the first curved 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, fluid can be quickly directed to the opposite downstream location, and flow resistance can be further reduced.
Preferably, as shown in fig. 3, a plurality of layers of flow guide plates 52 are arranged on the inner wall of the flue gas pipeline along the flow direction of flue gas, and the flow guide plates of adjacent layers are distributed in a staggered mode. Through the staggered distribution of the drainage plates of the adjacent rows, the flue gas can fully move to the opposite position in the flue gas pipeline, and the full and uniform mixing is ensured. FIG. 3 shows one drainage plate per layer. Of course, there may be more than one drainage plate per layer, for example, 3 drainage plates per layer.
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. With this arrangement, the air has less flow resistance on thorough mixing.
Preferably, the length of the first curved wall is greater than the length of the second curved wall.
Preferably, the total radian of the circular arcs connecting the drainage plates of the same layer with the inner wall is 150-180 degrees. This parameter set ensures thorough mixing while meeting the resistance requirements. For example, FIGS. 3 and 5 show one drainage plate per layer, with the total arc of one plate being 150 and 180. Of course, multiple drainage plates can be arranged on each layer, for example, three drainage plates are arranged on each layer in the angle of 150 and 180 degrees in total in FIG. 5.
As preferablely, A layer drainage plate sets up the polylith, sets up the interval between the A drainage plate, and the equidistant setting of A drainage plate, B layer are the adjacent row on A layer, follow the direction of flow and observe, and B layer drainage plate sets up the interval position department on A layer. Through the complementation of the positions of the flow guide plates of the adjacent layers, the flue gas can fully move to the opposite position in the flue gas pipeline, and the full 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 is only used as a distinction and is used as an adjacent layer.
Preferably, along the flow direction of flue gas, flue gas pipeline inner wall sets up a plurality of flow deflectors, and along the flow direction of flue gas, the distribution density of flow deflector is littleer and more. Because the mixing degree of the flue gas is better and better along with the continuous movement of the flue gas, the distribution density is required to be set to be smaller and smaller so as to reduce the flow resistance, and the temperature equalizing effect achieves the basically same effect on the aspects of reducing the resistance and saving the material cost.
Preferably, the distribution density of the flow guide plates is increased along the flowing direction of the smoke and along the flowing direction of the smoke. The effect is the result through a large amount of numerical simulation and experimental research, through research discovery, this law accords with the law of flue gas motion, on the degree that resistance further reduces and material cost saves, the samming effect reach basically the same effect.
Preferably, along the flow direction of flue gas, flue gas pipeline inner wall sets up a plurality of drainage plates, and along the flow direction of flue gas, the size of drainage plate is more and more littleer. 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 set to be smaller and smaller so as to reduce the flow resistance, and the temperature equalizing effect achieves the basically same effect on the aspects of reducing the resistance and saving the material cost.
As preferred, 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 range that the size of drainage plate is littleer and more constantly increases. The effect is the result through a large amount of numerical simulation and experimental research, through research discovery, this law accords with the law of flue gas motion, on the degree that resistance further reduces and material cost saves, the samming effect reach basically the same effect.
Through a large amount of numerical simulation and experimental study discovery, the angle and the size of drainage plate have very big influence to heat transfer and misce bene, drainage plate and inner wall contained angle are on the small side, can lead to mixing effect variation, and lead to the drainage plate size too big, influence the flow resistance, the contained angle is on the large side, it is not good to lead to stirring fluid effect, the resistance grow, mixing effect variation, the interval of drainage plate is too big, can lead to the vortex effect not good, the interval undersize can lead to increasing the movement resistance, consequently, this application has obtained nearest drainage plate structure size optimization relation through a large amount of data simulation and experiments.
Preferably, the length L2 of the first line between the connection point of the first curved wall and the inner wall and the intersection point 523, the length L1 of the second line between the connection point of the second curved wall and the inner wall and the intersection point 523, the acute angle between the first line and the inner wall is a2, the acute angle between the second line and the inside is a1, the distance S between adjacent wedge-shaped structures in the flow direction of the flue gas, i.e. the distance between the center points of the adjacent flow guide plates on the inner wall, and the center point is the midpoint of the connection line between the connection points of the first curved wall, the second curved wall and the inner wall, satisfy the following requirements:
n-a-b ln (M), wherein N ═ L1+ L2)/S, M ═ sin (a2)/sin (a 1); ln is a function of the logarithm of the number,
0.263<a<0.264，0.0829<b<0.0831；
preferably, 0.25< M <0.75,0.28< N <0.35,45< a1<75 °, 15< a2<45 °;
the diameter D of the pipeline 5 is 5000-.
The optimal design requirements of the drainage plate structure can be met by the various types. The structural optimization formula is a main improvement point of the invention, is the most optimized formula which is researched by a large number of numerical simulations and experiments, and is not common knowledge in the field.
More preferably, a is 0.2634 and b is 0.0830.
It is found in data simulation and experiment that the interval between the drainage plate must be greater than certain distance, otherwise can lead to the fluid to guide to opposite direction through last drainage plate, but if the interval undersize between the drainage plate, can lead to the flue gas to flow opposite, still not fully be full of whole pipeline, set up the drainage plate this moment, play not can not play mixed effect, the drainage plate only plays a baffling board effect, does not guide the effect of mixing, can only increase the flow resistance. Therefore, the design scheme of the minimum spacing of the drainage plate is provided through a great deal of research, and the design of the drainage plate has certain guiding significance.
The meeting point 523 is the vertical point on the inner wall, the line formed by the meeting point and the vertical point is the third line, the distance between the connecting point of the first bending wall and the inner wall and the vertical point is H, the acute angle formed by the first line and the third line is A3, the acute angle formed by the tangent of the first bending wall at the meeting point position and the axis of the flue gas pipeline is a4, the inner pipe diameter of the flue gas pipeline is R, and the distance S is designed in the following way:
(S/H)>a+b*Ln(T)，(S/R)2>c+d*Ln(T)；
wherein T ═ sin (A3)/sin (a4), 2.74< a <2.75,17.4< b <17.5, 1.998< c <1.999, 3.431< d <3.432, 30< A3<70 °, 20< a4<60 °; preferably 1.07< T < 1.30;
preferably, a is 2.743, b is 17.47, c is 1.9984, d is 0.4316;
according to the invention, through a large amount of experiments and numerical simulation, the minimum design distance of the drainage plate is obtained, and the resistance is reduced through the design distance, and meanwhile, 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 stacked on the fresh water bin 4 in parallel, the one-effect distiller 1 is arranged on the side of the one-effect distiller, a pipeline above the shell-and-tube heat exchanger 3 is divided into two paths and respectively introduced into the distillation chamber, the two paths are connected with the atomizing sprayer in the distillation chamber, the venturi sprayer is additionally arranged on the one-effect sprayer pipeline, the air exhaust end of the venturi sprayer is connected with the fresh water bin, and seawater is pumped into the shell part of the shell-and-tube heat exchanger 3 by a centrifugal pump after being filtered and then sprayed into the distillation chamber through the pipeline. The flue gas is led out by a bypass of a main engine exhaust pipeline, is blown into the lower part of the primary distiller 1 through a blower after being filtered, and is exhausted from the other end. The water vapor evaporated from the first-effect distiller 1 is communicated with the cold end at 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 position of the pipeline at the section close to the first-effect distiller so as to remove atomized seawater mixed in the steam; the same structure is also arranged on a pipeline connecting the double-effect distiller 2 and the shell-and-tube heat exchanger 3, and the functions are the same. The bottom ends of the two distiller separating plates in the inclined directions are connected with pipelines and finally merged into a 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 the flue gas lets in the hot junction of first effect distiller 1, the flue gas heat passes through high temperature heat pipe 11 and transmits the top hot junction, distill the cold sea water that sprays down, the leading-in cold junction of second effect distiller 2 of vapor that one effect distills, vapor meets cold liquefaction to become fresh water and flows in below fresh water storehouse 4 on the one hand, the liquefaction latent heat of vapor of the other hand transmits the hot junction of heat pipe top through second effect heat pipe 21, spray the sea water to the second effect and distill, vapor that two effects distill out lets in shell and tube heat exchanger 3 and cold sea water heat transfer, liquefaction becomes fresh water and flows in below fresh water storehouse 4 when preheating the sea water, therefore the source of fresh water is by two parts: one 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 of bitter water are merged and then discharged outwards.
The tank body of the single-effect distiller 1 is square, round corners are formed on the periphery of 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 end sealing cover can be detached, and the periphery of the upper end sealing cover is sealed by eight bolts; the top of the tank body is provided with a scale inhibitor storage tank, the inside of the tank body is provided with polyaspartic acid scale inhibitors, and the lower part of the tank body is connected with a sprayer in the distiller through a pipeline; atomizing sprayers are uniformly distributed in the circumferential direction of the scale inhibitor sprayer for spraying seawater; a high-temperature heat pipe array is vertically arranged in the distiller; the partition plate is obliquely arranged, and the surface of the upper half part is carved with flow guide lines so as to rapidly guide the bitter water out; and a glass wool material is filled between the two layers of partition plates for heat insulation. The lower part of the high-temperature heat pipe is welded with a transverse fin.
The whole structure of the double-effect distiller 2 is similar to that of the single-effect distiller, but the selection of the heat pipe and the selection of the hot end fin are different; the heat pipe of the double-effect distiller adopts a traditional heat pipe; the corrugated guide plate made of polyphenyl ether material is vertically arranged on the lower portion of the heat pipe and is inserted between the heat pipe arrays, so that turbulent flow is provided, steam and the heat pipe exchange heat efficiently, and the steam and the heat pipe smoothly flow into the fresh water bin below after being liquefied.
The shell-and-tube heat exchanger 3 is internally divided into a tube body and a shell, the tube body and the shell are mutually independent spaces, the tube body is a straight tube and is communicated from top to bottom, and steam in the double-effect distiller is introduced into the tube body from top to bottom; spoilers which are alternately arranged from left to right are arranged in the shell, and seawater is introduced from bottom to top; the steam exchanges heat with 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 and is arranged below the double-effect distiller and the shell-and-tube heat exchanger, meanwhile, the hole formed in the side surface of the fresh water bin is connected with the suction end of the venturi jet device on the seawater spraying pipeline through a hose, and when seawater flows, the fresh water bin can be pumped into negative pressure, so that the distilled water vapor can flow and be liquefied; meanwhile, due to the communication between the pipelines, the negative pressure can also reduce the pressure of the distillation end of the two-effect distiller, and the boiling point of the seawater is reduced.
The device is divided into two parts for controlling the seawater scaling, whether the spraying descaling is carried out is determined according to the scaling condition through sensor data during normal work, and sodium chloride adhered to a heat pipe during distillation is mainly discharged along with seawater through dissolution by increasing the seawater spraying amount and opening a bitter water outlet; when the sensor detects that excessive inorganic salt with low solubility such as magnesium sulfate and calcium sulfate exists on the surface of the heat pipe, the scale inhibitor can be automatically sprayed to carry out chemical descaling, and the scale can be removed by matching with the washing of seawater with large spraying amount.
Preferably, the heat exchanger further comprises a descaling agent storage tank, the descaling agent storage tank is located above the heat exchanger, descaling agent is stored in the descaling agent storage tank, and the descaling agent storage tank 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 normally operates, a diffuse reflection optical fiber sensor is used for sensing the scaling condition on the heat pipe, when the scaling quantity is overlarge, the spraying quantity of seawater is increased, a bitter water discharge electromagnetic valve is opened at the same time, the flushing time is timed through a timer, and soluble salts such as sodium chloride on the heat pipe are removed through a dissolving method; when the sensor detects that the scale formation amount is still in a high value after multiple times of washing, the polyaspartic acid scale inhibitor is sprayed to remove salts with low solubility, such as magnesium sulfate, calcium sulfate and the like, by a chelating dissolution and lattice distortion principle.
Preferably, the control system consists of a sensor, a microprocessor and a PID module; the sensors transmit data such as flue gas temperature, flue gas flow, seawater temperature, seawater flow, evaporation chamber temperature and the like to the microcontroller, the microcontroller accurately calculates the required flue gas flow and the seawater spraying amount according to an algorithm compiled in the microcontroller, and feeds the data back to the PID module, and the proportion-integral-differential closed-loop control system formed by the PID module realizes accurate control of the flue gas flow and the seawater spraying amount, so that the device can still efficiently and stably produce fresh water according to expected water yield under a complex external environment.
The heat exchange coefficients of the evaporation end and the condensation end of the heat pipe are respectively k1,k2(ii) a The heat exchange areas of the evaporation end and the condensation end of the heat pipe are respectively A1,A2(ii) a Calculating formula according to heat transfer coefficient of flat wall and heat transfer coefficient of rib wall
The heat exchange coefficient k of the evaporation end and the condensation 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 obtained by combining the heat transfer characteristic number into the formula1,k2(ii) a The temperature difference between the flue gas and the seawater obtained by the temperature sensor is delta t1,Δt2(ii) a Therefore, the heat flow Q of the flue gas can be calculated1＝k1A1Δt1(ii) a Heat quantity Q absorbed by sea water2＝k2A2Δt2(ii) a Then determining the smoke amount
Amount of seawater sprayed
The above embodiments are merely illustrative of the technical ideas and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.
Claims (8)
1. The utility model provides a sea water desalination device of ejector waste gas waste heat, a serial communication port, the device is including an effect distiller, two effect distiller, shell and tube type heat exchanger and fresh water storehouse, two effect distiller is connected to an effect distiller, and two effect distiller connects shell and tube type heat exchanger, fresh water storehouse sets up the lower part at two effect distiller and shell and tube type heat exchanger, the device still includes the venturi ejector, and it is installed on the shower pipeline of an effect distiller, and fresh water storehouse is connected to the end of bleeding.
2. The seawater desalination apparatus of claim 1 wherein the fresh water sump is arranged below the double-effect distiller and the shell-and-tube heat exchanger, and is connected with the suction end of the venturi ejector on the seawater spray pipeline through a hose at the side opening.
3. The seawater desalination apparatus of claim 1, wherein the filtered flue gas is blown into a lower portion of the single-effect distiller by a blower and then discharged from the other end.
4. The seawater desalination apparatus of claim 1, wherein the first-effect distiller is provided with a first-effect heat pipe and a first-effect splitter plate, the first-effect splitter plate divides the first-effect heat pipe into a hot end at the upper part and a cold end at the lower part, the second-effect distiller is provided with a second-effect heat pipe and a second-effect splitter plate, the second-effect splitter plate divides the second-effect heat pipe into a hot end at the upper part and a cold end at the lower part, the flue gas is introduced into the cold end of the first-effect distiller, the heat of the flue gas is transferred to the hot end at the upper part through the cold end of the high-temperature heat pipe to distill cold seawater sprayed down, the vapor distilled out by the first-effect distiller is introduced into the cold end of the second-effect distiller, on the one hand, the vapor is liquefied into fresh water to flow into the fresh water bin at the lower part when encountering cold, on the other hand, the latent heat of liquefaction of the vapor is transferred to the hot end at the upper part of the second-effect heat pipe through the second-effect heat pipe to distill the spray seawater sprayed from the second-effect distiller, the water vapor distilled out by the double-effect distiller is introduced into a shell-and-tube heat exchanger, exchanges heat with cold seawater in the shell-and-tube heat exchanger, and is liquefied into fresh water while preheating the seawater, and the fresh water flows into a fresh water bin below.
5. The seawater desalination apparatus of claim 4, wherein the shell-and-tube heat exchanger is vertically disposed above the fresh water sump, seawater is introduced into the shell, vapor distilled from the double-effect distiller is absorbed into the tube, the vapor is liquefied in the tube and flows into the fresh water sump below, and at the same time, the seawater in the shell is preheated, and the preheated seawater enters the single-effect distiller and the double-effect distiller through the spraying device.
6. The seawater desalination apparatus of claim 4, further comprising a spray pipeline, wherein an inlet of the spray pipeline is connected with the seawater outlet of the shell-and-tube heat exchanger, and an outlet of the spray pipeline is connected with the first-effect distiller and the second-effect distiller.
7. The seawater desalination apparatus of claim 1, comprising a temperature equalization device disposed on a conduit for flue gas to enter the single-effect distiller.
8. A seawater desalination device based on ship waste gas waste heat is characterized by comprising a primary effect distiller, a secondary effect distiller, a shell-and-tube heat exchanger and a fresh water bin.
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| GB939188A (en) * | 1961-05-13 | 1963-10-09 | Nirex Ingenior Aktieselskab | Improvements in and relating to a vacuum distillation plant for the production of fresh water from sea water onboard ships |
| 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 |
| CN101955238A (en) * | 2010-10-08 | 2011-01-26 | 河北工业大学 | Seawater desalting method and device |
| CN104030385A (en) * | 2014-06-30 | 2014-09-10 | 上海伏波环保设备有限公司 | Indirect low-temperature multi-effect seawater desalination system by using waste heat of exhaust gas of ship engine |
| CN105417606A (en) * | 2015-12-16 | 2016-03-23 | 鹤壁汽车工程职业学院 | Multi-effect distillation and multi-stage flash evaporation solar sea water desalination method |
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2020
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB939188A (en) * | 1961-05-13 | 1963-10-09 | Nirex Ingenior Aktieselskab | Improvements in and relating to a vacuum distillation plant for the production of fresh water from sea water onboard ships |
| CN2280708Y (en) * | 1996-12-31 | 1998-05-06 | 江苏理工大学 | Heat-pipe type sea-water desalinating device |
| CN101955238A (en) * | 2010-10-08 | 2011-01-26 | 河北工业大学 | Seawater desalting method and 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 |
| CN104030385A (en) * | 2014-06-30 | 2014-09-10 | 上海伏波环保设备有限公司 | Indirect low-temperature multi-effect seawater desalination system by using waste heat of exhaust gas of ship engine |
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