CN102381734A - Low-temperature multi-effect seawater distillation and desalination system and method for sweater desalination - Google Patents
Low-temperature multi-effect seawater distillation and desalination system and method for sweater desalination Download PDFInfo
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- CN102381734A CN102381734A CN2011102887228A CN201110288722A CN102381734A CN 102381734 A CN102381734 A CN 102381734A CN 2011102887228 A CN2011102887228 A CN 2011102887228A CN 201110288722 A CN201110288722 A CN 201110288722A CN 102381734 A CN102381734 A CN 102381734A
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- 239000013535 sea water Substances 0.000 title claims abstract description 90
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000004821 distillation Methods 0.000 title claims abstract description 28
- 230000000694 effects Effects 0.000 claims abstract description 90
- 239000011552 falling film Substances 0.000 claims abstract description 58
- 239000010408 film Substances 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 239000007788 liquid Substances 0.000 claims description 22
- 239000002826 coolant Substances 0.000 claims description 19
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- 238000001704 evaporation Methods 0.000 claims description 16
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000005086 pumping Methods 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 7
- 230000001151 other effect Effects 0.000 claims description 2
- 239000002356 single layer Substances 0.000 claims description 2
- 230000002311 subsequent effect Effects 0.000 claims 2
- 230000009290 primary effect Effects 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 24
- 239000012267 brine Substances 0.000 description 22
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 22
- 238000001816 cooling Methods 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000007872 degassing Methods 0.000 description 4
- 239000012153 distilled water Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 239000002455 scale inhibitor Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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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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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a low-temperature multi-effect seawater distillation and desalination system and a method for sweater desalination, which are used for improving performance of the low-temperature multi-effect seawater distillation and desalination system. The low-temperature multi-effect seawater distillation and desalination system comprises at least two effect evaporators in serial connection, a falling-film condenser connected with a terminal effect evaporator, a heat pump device, a vacuuming device and a compelling condenser. The heat pump device is respectively connected with a primary effect evaporator and any one effect evaporator, the vacuuming device is respectively connected with the primary effect evaporator and the falling-film condenser, and the compelling condenser is parallelly connected with the falling-film condenser to assist the down-film condenser in condensing secondary steam generated by the terminal effect evaporator.
Description
Technical Field
The invention relates to the technical field of seawater desalination, in particular to a low-temperature multi-effect distillation seawater desalination system and a seawater desalination method.
Background
The low-temperature multi-effect distillation seawater desalination technology is characterized in that a series of evaporators are connected in series, a certain amount of steam is input to the evaporators for multiple times of evaporation and condensation, and the evaporation temperature of the latter effect is lower than that of the former effect, so that the desalination process of distilled water with the quantity of the steam being multiple times is obtained.
In the low-temperature multi-effect distillation process, feed seawater is preheated and non-condensable gas is removed in a condenser, a certain amount of non-condensable gas is released when the seawater is gasified in an evaporator, and in addition, air also leaks into the evaporator to become the non-condensable gas in a vacuum operation environment. The presence of these non-condensable gases affects the efficiency of heat transfer and causes corrosion, and therefore these non-condensable gases and small amounts of water vapor must be removed from the system by a vacuum extractor to maintain and ensure a vacuum level in which the system operates.
There are various conventional methods for removing non-condensable gas from seawater, and one of the methods includes: the feed seawater enters the evaporators without degassing, a large amount of non-condensable gas is degassed in each evaporator, namely, the vacuumizing device is directly connected with the evaporators, and the non-condensable gas is pumped out. This requires that the heat exchange tube of the evaporator must be made of a material with high corrosion resistance and high heat conductivity, and a vacuum-pumping device with a large air-pumping capacity is also required, and the arrangement of the air-pumping point of the system is also complicated, which results in a sharp increase in equipment investment and operation cost.
The other method is to preheat and degas the feed seawater by adopting a falling film condenser, the preheating and degassing amount of the feed seawater is reduced, the power consumption of a system is also reduced, and a heat exchange tube of an evaporator does not need to be made of a material with high corrosion resistance and high heat conductivity coefficient. However, in this method, in order to condense all the vapor of the last-effect evaporator, an excessive amount of feed seawater is still required to be introduced into the falling film condenser. Therefore, a large amount of feed seawater forms a part of feed liquid after being heated and can only be discharged outside, and great waste of materials and heat is caused. Therefore, the low-temperature multi-effect distillation seawater desalination system cannot flexibly adapt to the temperature change of seawater. Meanwhile, because excessive feed seawater is degassed in the falling film condenser, the quantity of non-condensable gas in the system is still large.
Therefore, the existing low-temperature multi-effect distillation seawater desalination system has high cost for removing the non-condensable gas in seawater, is complex and causes resource waste, so that the performance of the low-temperature multi-effect distillation seawater desalination system needs to be further improved.
Disclosure of Invention
The embodiment of the invention provides a low-temperature multi-effect distilled seawater desalination system and a seawater desalination method, which are used for saving resources used in the process of removing non-condensable gas in seawater by the low-temperature multi-effect distilled seawater desalination system and improving the performance of the low-temperature multi-effect distilled seawater desalination system.
The embodiment of the invention provides a low-temperature multi-effect distillation seawater desalination system, which comprises: the evaporator comprises at least two effect evaporators connected in series, a falling film condenser connected with a last effect evaporator, a heat pump device respectively connected with the first effect evaporator and any other effect evaporator, a vacuum pumping device respectively connected with the first effect evaporator and the falling film condenser, and a forced condenser connected with the falling film condenser in parallel, wherein the forced condenser is used for assisting the falling film condenser to condense secondary steam generated by the last effect evaporator.
The embodiment of the invention provides a method for desalinating seawater by a low-temperature multi-effect distillation seawater desalination system, wherein a falling film condenser and a forced condenser in the low-temperature multi-effect distillation seawater desalination system are connected in parallel and then are connected with an end-effect evaporator in an evaporator with at least two effects connected in series, and the method comprises the following steps:
the falling film condenser condenses secondary steam input from the last effect evaporator to generate product water, preheats feed seawater outside the heat exchange pipe by latent heat released in the condensation process, deaerates the preheated seawater to form feed liquid, and inputs the feed liquid into the at least two-effect series-connected evaporators;
the forced condenser condenses secondary steam input from the last effect evaporator by using a cooling medium to generate product water, wherein the cooling medium comprises: cooling water or seawater is circulated.
In the embodiment of the invention, a strong condenser is added in the low-temperature multi-effect distillation seawater desalination system and is connected with a final-effect evaporator after being connected in parallel with a falling film condenser, so that secondary steam generated by the final-effect evaporator can enter the falling film condenser and the strong condenser respectively in two ways according to the change of the temperature of fed seawater, the secondary steam entering the falling film condenser only needs to be condensed by the fed seawater required by the system, and the rest secondary steam is condensed by the strong condenser by the existing cooling medium, so that the feed seawater quantity of the system is reduced, the phenomenon that all secondary steam generated by the final-effect evaporator is condensed by excessive fed seawater is avoided, resources used in the process of removing non-condensable gas in seawater by the low-temperature multi-effect distillation seawater desalination system are saved, and the performance of the low-temperature multi-effect distillation seawater desalination system is improved.
Drawings
FIG. 1 is a schematic diagram of a low-temperature multi-effect distillation seawater desalination system according to an embodiment of the present invention.
The reference numbers in the figures illustrate:
1-9-an evaporator; 10-a falling film condenser; 11-a forced condenser;
12-19-strong brine flash tank; 20-strong brine buffer tank; 21-28-product water flash tank; 29-product water buffer tank; 30-a condensate buffer tank;
31-a vacuum-pumping device; 32-a heat pump device; 33-feed seawater pump;
34-35-strong brine pump; 36-condensate pump; 37-product water pump; 38-concentrated brine pump;
39-strong brine heat exchanger; 40-product water heat exchanger;
41-feed seawater; 42-falling film condenser and forced cooling condenser connecting pipe
Detailed Description
In the embodiment of the invention, a strong condenser is added in the low-temperature multi-effect distillation seawater desalination system, and the strong condenser is connected with the last-effect evaporator after being connected in parallel with the falling film condenser, so that secondary steam generated by the last-effect evaporator can be condensed by the falling film condenser and the strong condenser together. The falling film condenser only needs to utilize feed seawater to condense secondary steam input from the last effect evaporator, and the rest secondary steam is condensed by the forced condenser by adopting the existing cooling medium, wherein the existing cooling medium comprises circulating cooling water or seawater. Thus, the amount of seawater fed into the system is reduced, and the phenomenon that the excessive seawater is used for condensing all secondary steam generated by the last-effect evaporator is avoided.
The embodiments of the present invention will be described in further detail with reference to the drawings attached hereto.
Referring to fig. 1, in the embodiment, the low-temperature multi-effect distillation seawater desalination system comprises 1-9 effect evaporators, wherein the evaporators are divided into 3 effect groups, the 1 st-2 effects are the 1 st effect group, the 3 rd-5 th effects are the 2 nd effect group, and the 6 th-9 th effects are the 3 rd effect group. The 1-9 effect evaporators are connected in series, namely a shell of the evaporator with the previous effect is connected with a heat exchange tube bundle of the evaporator with the next effect, the evaporation temperature of the evaporator with the previous effect is higher than that of the evaporator with the next effect, and the evaporation temperature of the evaporator with the first effect is not higher than 70 ℃.
The 9 th effect evaporator 9 is an end effect evaporator and is connected with the falling film condenser 10, and the forced cooling condenser 11 is connected with the falling film condenser 10 in parallel and then is connected with the end effect evaporator.
Generally, the passage of the last effect evaporator connected with the falling film condenser is provided with one, two or more pipe orifices, and the steam passage of the forced condenser is connected with the last effect evaporator through the pipe orifices. Preferably, the passage of the last effect evaporator to the falling film condenser has 1 to 6 pipe openings, so that the force condenser has 1 to 6 pipes and the passage connection between the last effect evaporator and the falling film condenser.
Here, the intensive condenser 11 is connected to the passage through 3 pipes 42.
Taking fig. 1 as an example, a shell-and-tube heat exchanger is used for the falling film condenser 10 and the intensive condenser 11. The falling film condenser 10 is a main condenser, and the forced cooling condenser 11 is an auxiliary condenser. Namely a strong condenser 11 and an auxiliary falling film condenser 10, to condense the secondary steam generated by the last effect evaporator 9.
The feed seawater 41 enters the falling film condenser 10 at a fixed temperature after heat exchange through the strong brine heat exchanger 39 and the product water heat exchanger 40 according to the temperature. The falling film condenser 10 employs a shell-and-tube heat exchanger comprising: the shell, the heat exchange tube bundle of arranging of bilayer that is located the casing, the spray set who is located the heat exchange tube bundle top, the product water of condensation is collected to the pipe case that is located the heat exchange tube bundle both ends, and the charge-in liquid is collected to the catch tray that is located the heat exchange tube bundle below.
The feed seawater 41 is preheated to a fixed temperature and degassed, and the feed seawater becomes the feed liquid required by the evaporators 1-9.
After the scale inhibitor is added into the feed liquid, the feed liquid is pumped to the evaporators 6-9 of the 3 rd effect group by a feed sea water pump 33, the feed liquid is sprayed out of the spraying devices of the evaporators 6-9, after the evaporation process is finished, the concentrated residual feed liquid is pumped into the evaporators 3-5 of the 2 nd effect group by a concentrated brine pump 34, and the spraying and evaporation processes are repeated in the 2 nd effect group. The remaining feed is then pumped forward by concentrated brine pump 35 to effect 1 until finally leaving the effect as a concentrate.
The heat pump device 32 is connected with the 1 st effect evaporator and pumps power steam into the 1 st effect evaporator 1, and here, the heat pump device 32 is also connected with the 6 th effect evaporator, so that low-pressure steam is pumped from the 6 th effect evaporator 6 and then mixed with the power steam to form raw steam which enters the heat exchange pipe of the 1 st effect evaporator 1.
After raw steam is input into a heat exchange pipe of the 1 st-effect evaporator 1, namely the first-effect evaporator, the raw steam in the heat exchange pipe is condensed by using feed liquid outside the heat exchange pipe to generate condensed water, and the condensed water is introduced into a condensed water buffer tank 30. Meanwhile, the latent heat released in the condensation process causes evaporation which is basically the same as the condensation amount to be generated outside the tube, namely the latent heat released in the condensation process evaporates the feed liquid outside the heat exchange tube to form secondary steam. Because the shell of the evaporator of the former effect is connected with the heat exchange tube bundle of the evaporator of the latter effect, the formed secondary steam is introduced into the heat exchange tube of the evaporator 2 of the 2 nd effect after passing through the strong brine drop separator to ensure the purity of the distilled water.
The second effect evaporator 2 condenses the secondary steam input in the heat exchange tube to generate product water, and the latent heat released in the condensation process evaporates the feed liquid outside the heat exchange tube to form secondary steam, and the secondary steam is introduced into the heat exchange tube of the third effect evaporator 3.
By analogy, this evaporation and condensation process is repeated along each effect of the series of evaporators, each effect producing a significant amount of product water until the second vapor is formed in evaporator 9 of effect 9.
Since the forced condenser 11 is connected to the 9 th effect evaporator 9 after being connected in parallel to the falling film condenser 10, part of the secondary steam flows into the heat exchange tubes of the falling film condenser 10. The falling film condenser 10 condenses the secondary steam in the heat exchange tubes with the feed seawater and forms product water. At the same time, the latent heat released by condensation heats the feed seawater to a fixed temperature, i.e. preheats the feed seawater.
The remaining secondary steam is automatically distributed to the intensive condenser 11 through the pipe 42. The forced condenser 11 condenses the secondary steam with a cooling medium to generate product water. Here, when the shell-and-tube heat exchanger is used as the forced condenser 11, the heat exchange tube bundle is horizontally arranged in the shell. The secondary steam in the forced condenser is positioned outside the tubes of the heat exchange tube bundle, and the cooling medium, namely the circulating cooling water is positioned in the tubes of the heat exchange tube bundle, so that the residual secondary steam in the 9 th-effect evaporator 9 is condensed, and the residual heat is transferred to the circulating cooling water.
The forced condenser 11 is connected with the falling film condenser 10 through a pipeline 42, no valve is arranged on the pipeline, and the secondary steam quantity of the 9 th effect evaporator 9 entering the forced condenser is automatically distributed according to the flow of a cooling medium of the forced condenser.
As shown in FIG. 1, the produced product water and the concentrated brine respectively flow into product water flash tanks 21-28 and concentrated brine flash tanks 12-19, each flash tank is connected to the shell side of the evaporator, wherein the product water flash tanks 21-28 and the concentrated brine flash tanks 12-19 respectively correspond to the evaporators 2-9. And the product water flash tank 29 and the concentrated brine flash tank 20 correspond to the falling film condenser 11.
Therefore, the product water and the strong brine flow in a step shape and are cooled by flash evaporation step by step, and the total efficiency of the system is improved by the released heat. The cooled product water and the concentrated brine are finally pumped by corresponding product water pumps 37 and concentrated brine pumps 38 respectively, and the condensed water is sent out by a condensed water pump 36.
Some non-condensable gas is still in the form of gas, and the non-condensable gas cannot be condensed into liquid, so that the non-condensable gas needs to be extracted from each heat exchange tube and flows to the other evaporator from the plate holes of the evaporator with one effect. These non-condensable gases are enriched in the effect 1 evaporator and falling film condenser 10 and are evacuated from the evacuation ports by means of a 3-stage vacuum 31.
As shown in fig. 1, a vacuum extractor 31 is connected to the first-effect evaporator 1, the falling film condenser 10, and the intensive condenser 11, respectively, to extract noncondensable gas and a small amount of water vapor in the system.
In the embodiment of the present invention, the intensive condenser 11 is a shell-and-tube heat exchanger, however, the intensive condenser 11 may further include: a plate heat exchanger. Wherein, when the amount of steam entering the forced condenser 11 is small, the forced condenser 11 can adopt a plate heat exchanger. When the amount of steam entering the forced condenser 11 is large, the forced condenser uses a shell-and-tube heat exchanger. When the forced condenser 11 is a shell-and-tube heat exchanger, the heat exchange tube bundles in the shell 11 of the forced condenser are horizontally arranged, the secondary steam entering the forced condenser flows in the shell, and the cooling medium entering the forced condenser flows in the heat exchange tube bundles. Because the cooling medium flows in the heat exchange tube bundle, the flowing speed of the cooling medium can be high, and the speed of condensing the secondary steam by the intensive condenser 11 is increased.
In the above embodiments, the falling film condenser is a shell-and-tube heat exchanger, and the heat exchange tube bundles in the falling film condenser may be arranged in a single layer or in multiple layers. Wherein, the feed seawater sprayed out by the spraying device flows downwards in a film shape outside the heat exchange tube bundle.
In this embodiment, the vacuum pumping device is a single-stage or multi-stage steam jet pump, and is generally connected to the first-effect evaporator and the falling film condenser, respectively, and may also be connected to the forced cooling condenser. The vacuum pumping device pumps out non-condensable gas, a small amount of water vapor and leaked air in the evaporator and the condenser so as to ensure and maintain the requirement of the system on the vacuum degree.
The heat pump device is a fixed nozzle type or adjustable nozzle type steam jet pump and can be respectively connected with the first-effect evaporator and any other one-effect evaporator, so that the heat pump device can suck partial secondary steam of the last-effect evaporator or a certain middle-effect evaporator and then mix the secondary steam with power steam to enter a heat exchange pipe in the first-effect evaporator. Thus, part of the secondary steam of the low-temperature effect section returns to the first-effect evaporator through the compression and circulation of the heat pump, the heat efficiency of the process is obviously improved, and the performance ratio of the device is improved.
In the above embodiments, the low-temperature multi-effect distillation seawater desalination system includes a 9-effect evaporator, but the embodiment of the present invention is not limited thereto, and the system may include only a 2-effect evaporator, or a multi-effect evaporator, for example: 20-effect evaporators. The multiple-effect evaporators may be grouped, each group of evaporators corresponding to a concentrated brine pump, or, without grouping the multiple-effect evaporators, each evaporator corresponding to a concentrated brine pump.
According to the embodiment, after the falling film condenser connected with the forced condenser in parallel is added in the low-temperature multi-effect distillation seawater desalination system, the working process of each effect evaporator is unchanged in the seawater desalination process, and the working process of the falling film condenser comprises the following steps: condensing secondary steam input from the last effect evaporator to generate product water, preheating feed seawater outside the heat exchange pipe by using latent heat released in the condensation process, degassing the preheated seawater to form feed liquid, and inputting the feed liquid into at least two-effect series-connected evaporators.
The working process of the forced condenser comprises the following steps: and condensing the secondary steam input from the last-effect evaporator by using a cooling medium to generate product water.
The specific seawater desalination process comprises the following steps: feed seawater, which forms the feed liquid required for the effect groups of the evaporators, is preheated and degassed in the falling film condenser. The feeding liquid is introduced into each effect evaporator of the last effect group after being added with the scale inhibitor, the spraying device sprays and distributes the feeding liquid to the top discharge pipe in each evaporator, and in the process of freely flowing downwards along the top discharge pipe in a film mode, a part of seawater is vaporized into secondary steam due to the absorption of latent heat of condensed steam in the evaporator. The slightly concentrated residual feed solution is pumped into the next effect group of evaporators, which group is operated at a somewhat higher temperature than the previous group, and the evaporation and spraying process is repeated in the new group. The remaining feed liquid is then pumped forward until finally leaving the effect group at the highest temperature in the form of a concentrate.
Raw steam consisting of power steam is input into the evaporator with the highest temperature and one effect, namely the heat exchange pipe of the first-effect evaporator, and when condensation occurs in the pipe, evaporation with the same amount as the condensation is generated outside the pipe, namely latent heat released by condensation is used for evaporating feed water to generate secondary steam. The generated secondary steam is introduced into the heat exchange pipe of the next effect evaporator after passing through a strong brine drop separator to ensure the purity of distilled water, and the operation temperature and pressure of the 2 nd effect evaporator are slightly lower than those of the first effect. The evaporation and condensation process is repeated along a series of evaporators all the time, each evaporator effect generates a considerable amount of product water, part of secondary steam generated by the last evaporator effect flows into a heat transfer pipe of the falling film condenser, the released latent heat heats the input seawater to a fixed temperature, and the rest secondary steam enters the intensive condenser for condensation and transfers the waste heat to a cooling medium. Wherein the cooling medium includes: cooling water or seawater is circulated.
The produced product water and strong brine respectively flow into a series of flash tanks, and each flash tank is connected to the shell side of the evaporator, so that the product water and the strong brine flow in a step shape and are subjected to flash cooling step by step, and the discharged heat improves the total efficiency of the system. And finally, pumping the cooled product water and the strong brine by using corresponding water pumps respectively, and pumping out condensed water by using a condensed water pump.
Non-condensable gases, i.e., non-condensable gases, are drawn from each condenser tube and flow from the plate holes of one evaporator effect to the other evaporator effect. These non-condensable gases are enriched in the evaporator and falling film condenser and are evacuated by means of a vacuum extractor.
In the embodiment of the invention, a strong condenser is added in a low-temperature multi-effect distillation seawater desalination system and is connected with a last-effect evaporator after being connected in parallel with a falling film condenser, so that secondary steam generated by the last-effect evaporator can enter the falling film condenser and the strong condenser respectively in two ways according to the change of the temperature of feed seawater, the secondary steam entering the falling film condenser only needs to be condensed by the feed seawater required by the system, and the rest secondary steam is condensed by the strong condenser by the existing cooling medium, so that the feed seawater quantity of the system is reduced, and the condensation of all the secondary steam generated by the last-effect evaporator by using excessive feed seawater is avoided. The resources used in the process of removing the non-condensable gas in the seawater by the low-temperature multi-effect distillation seawater desalination system are saved, and the performance of the low-temperature multi-effect distillation seawater desalination system is improved.
Meanwhile, the amount of seawater fed into the system is reduced, so that the degassing amount of the fed seawater is reduced. The reduction of the air exhaust amount reduces the capacity of a vacuum extractor, simplifies the non-condensable gas point pumping of the system, improves the heat exchange efficiency of an evaporator, lightens the corrosion of equipment and the like, improves the stability and reliability of the system, and reduces the water making cost of the system
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. A low-temperature multi-effect distillation seawater desalination system comprises: the evaporimeter of at least two effect series connection, the falling film condenser of being connected with last effect evaporimeter, the heat pump device who is connected respectively with first effect evaporimeter and all the other arbitrary effect evaporimeters, and with first effect evaporimeter with the evacuating device that the falling film condenser is connected respectively, its characterized in that still includes:
and the forced condenser is connected with the falling film condenser in parallel and assists the falling film condenser to condense the secondary steam generated by the last effect evaporator.
2. The system of claim 1,
the falling film condenser is connected with the last effect evaporator through a channel, and at least one pipe orifice is arranged on the channel;
and the steam channel of the forced condenser is connected with the end-effect evaporator through the pipe orifice.
3. The system of claim 1, wherein the shell of the evaporator of the previous effect is connected to the heat exchange tube bundle of the evaporator of the subsequent effect, and the evaporation temperature of the evaporator of the previous effect is greater than the evaporation temperature of the evaporator of the subsequent effect, and the evaporation temperature of the evaporator of the first effect is no more than 70 degrees celsius.
4. The system of claim 1,
the falling film condenser is a shell-and-tube heat exchanger and comprises: the device comprises a shell, heat exchange tube bundles arranged in a single layer or multiple layers in the shell, a spraying device arranged above the heat exchange tube bundles, tube boxes arranged at two ends of the heat exchange tube bundles and used for collecting condensed product water, and a collecting tray arranged below the heat exchange tube bundles and used for collecting feed liquid; wherein,
the feed seawater sprayed out by the spraying device flows downwards in a film shape outside the heat exchange tube bundle.
5. The system of claim 4, wherein the shell of the last effect evaporator is coupled to a heat exchange tube bundle of the falling film condenser.
6. The system of claim 1 or 2,
the intensive condenser comprises: when the forced condenser is a shell-and-tube heat exchanger, the heat exchange tube bundles in the shell of the forced condenser are horizontally arranged, secondary steam entering the forced condenser flows in the shell, and a cooling medium entering the forced condenser flows in the heat exchange tube bundles.
7. The system of claim 6,
the cooling medium used by the intensive condenser comprises: cooling water or seawater is circulated.
8. The system of claim 1,
the vacuum pumping device is a single-pole or multi-stage steam jet pump and is also connected with the forced condenser to pump noncondensable gas and a small amount of water vapor in the forced condenser, the first-effect evaporator and the falling film condenser.
9. The system as claimed in claim 1, wherein the heat pump device is a fixed nozzle type or adjustable nozzle type steam jet pump, and part of secondary steam in any one of the other effect evaporators is extracted and then mixed with motive steam to enter a heat exchange pipe in the first effect evaporator.
10. A method for desalinating seawater by a low-temperature multi-effect distillation seawater desalination system is characterized in that a falling film condenser and a forced condenser in the low-temperature multi-effect distillation seawater desalination system are connected in parallel and then are connected with an end-effect evaporator in an evaporator with at least two effects connected in series, and the method comprises the following steps:
the falling film condenser condenses secondary steam input from the last effect evaporator to generate product water, preheats feed seawater outside the heat exchange pipe by latent heat released in the condensation process, deaerates the preheated seawater to form feed liquid, and inputs the feed liquid into the at least two-effect series-connected evaporators;
the forced condenser condenses secondary steam input from the last effect evaporator by using a cooling medium to generate product water, wherein the cooling medium comprises: cooling water or seawater is circulated.
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| CN2011102887228A CN102381734A (en) | 2011-09-26 | 2011-09-26 | Low-temperature multi-effect seawater distillation and desalination system and method for sweater desalination |
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| CN2011102887228A CN102381734A (en) | 2011-09-26 | 2011-09-26 | Low-temperature multi-effect seawater distillation and desalination system and method for sweater desalination |
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Cited By (14)
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| CN103030185A (en) * | 2012-12-19 | 2013-04-10 | 中国电子工程设计院 | Low-temperature multi-effect sea water desalinization system |
| CN103058301A (en) * | 2013-01-15 | 2013-04-24 | 中国电子工程设计院 | Horizontal flash tank and low-temperature multi-effect distillation seawater desalination system |
| CN103073142A (en) * | 2013-01-11 | 2013-05-01 | 中国电子工程设计院 | Multiple-effect-group, low-temperature and multiple-effect distilled seawater desalination system |
| CN103073141A (en) * | 2013-01-10 | 2013-05-01 | 中国电子工程设计院 | Low-temperature multi-effect distilled seawater desalination system with variable effect groups |
| CN103086451A (en) * | 2013-01-30 | 2013-05-08 | 大连理工大学 | Multi-effect evaporative sea water desalinating device with hybrid process |
| CN103508502A (en) * | 2013-09-22 | 2014-01-15 | 汉盛（上海）海洋装备技术股份有限公司 | Two-stage cryogenic-distillation sea water desalination process utilizing waste heat of marine main engine and generator |
| CN108168132A (en) * | 2018-02-13 | 2018-06-15 | 广州中国科学院先进技术研究所 | A kind of heat pipe coupling phase change cold-storage produces the system and its technique of injection water |
| CN108325227A (en) * | 2018-04-10 | 2018-07-27 | 上海优华系统集成技术股份有限公司 | A kind of system and its processing method to heat recovery and utilization in multi-effect evaporation system |
| CN108793292A (en) * | 2018-07-12 | 2018-11-13 | 中国恩菲工程技术有限公司 | Utilize the heat-exchanger rig of waste heat |
| CN112939124A (en) * | 2021-03-30 | 2021-06-11 | 上海核工程研究设计院有限公司 | Novel low-temperature exhaust-heat seawater desalination system and method |
| CN112978829A (en) * | 2021-03-31 | 2021-06-18 | 天津国投津能发电有限公司 | Low-temperature multi-effect distillation seawater desalination system and process method thereof |
| CN113845163A (en) * | 2021-11-05 | 2021-12-28 | 广东闻扬环境科技有限公司 | Seawater desalination system and seawater desalination method |
| CN114804266A (en) * | 2022-05-18 | 2022-07-29 | 天津国投津能发电有限公司 | Falling film condenser of low-temperature multi-effect distillation seawater desalination system |
| CN115367825A (en) * | 2021-05-19 | 2022-11-22 | 中国石油化工股份有限公司 | Seawater desalination and condensation system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103030185A (en) * | 2012-12-19 | 2013-04-10 | 中国电子工程设计院 | Low-temperature multi-effect sea water desalinization system |
| CN103073141A (en) * | 2013-01-10 | 2013-05-01 | 中国电子工程设计院 | Low-temperature multi-effect distilled seawater desalination system with variable effect groups |
| CN103073141B (en) * | 2013-01-10 | 2014-08-20 | 中国电子工程设计院 | Low-temperature multi-effect distilled seawater desalination system with variable effect groups |
| CN103073142A (en) * | 2013-01-11 | 2013-05-01 | 中国电子工程设计院 | Multiple-effect-group, low-temperature and multiple-effect distilled seawater desalination system |
| CN103058301A (en) * | 2013-01-15 | 2013-04-24 | 中国电子工程设计院 | Horizontal flash tank and low-temperature multi-effect distillation seawater desalination system |
| CN103086451A (en) * | 2013-01-30 | 2013-05-08 | 大连理工大学 | Multi-effect evaporative sea water desalinating device with hybrid process |
| CN103508502A (en) * | 2013-09-22 | 2014-01-15 | 汉盛（上海）海洋装备技术股份有限公司 | Two-stage cryogenic-distillation sea water desalination process utilizing waste heat of marine main engine and generator |
| CN108168132B (en) * | 2018-02-13 | 2020-08-18 | 广州中国科学院先进技术研究所 | System and process for preparing injection water by coupling heat pipe with phase change cold accumulation |
| CN108168132A (en) * | 2018-02-13 | 2018-06-15 | 广州中国科学院先进技术研究所 | A kind of heat pipe coupling phase change cold-storage produces the system and its technique of injection water |
| CN108325227A (en) * | 2018-04-10 | 2018-07-27 | 上海优华系统集成技术股份有限公司 | A kind of system and its processing method to heat recovery and utilization in multi-effect evaporation system |
| CN108325227B (en) * | 2018-04-10 | 2024-04-16 | 上海优华系统集成技术股份有限公司 | System for recycling heat in multi-effect evaporation system and treatment method thereof |
| CN108793292B (en) * | 2018-07-12 | 2024-01-05 | 中国恩菲工程技术有限公司 | Heat exchange device utilizing waste heat |
| CN108793292A (en) * | 2018-07-12 | 2018-11-13 | 中国恩菲工程技术有限公司 | Utilize the heat-exchanger rig of waste heat |
| CN112939124A (en) * | 2021-03-30 | 2021-06-11 | 上海核工程研究设计院有限公司 | Novel low-temperature exhaust-heat seawater desalination system and method |
| CN112978829B (en) * | 2021-03-31 | 2024-03-12 | 天津国投津能发电有限公司 | Low-temperature multi-effect distillation seawater desalination system and process method thereof |
| CN112978829A (en) * | 2021-03-31 | 2021-06-18 | 天津国投津能发电有限公司 | Low-temperature multi-effect distillation seawater desalination system and process method thereof |
| CN115367825A (en) * | 2021-05-19 | 2022-11-22 | 中国石油化工股份有限公司 | Seawater desalination and condensation system and method |
| CN113845163A (en) * | 2021-11-05 | 2021-12-28 | 广东闻扬环境科技有限公司 | Seawater desalination system and seawater desalination method |
| CN113845163B (en) * | 2021-11-05 | 2024-04-19 | 广东闻扬环境科技有限公司 | Seawater desalination system and seawater desalination method |
| CN114804266A (en) * | 2022-05-18 | 2022-07-29 | 天津国投津能发电有限公司 | Falling film condenser of low-temperature multi-effect distillation seawater desalination system |
| CN114804266B (en) * | 2022-05-18 | 2023-02-28 | 天津国投津能发电有限公司 | Falling film condenser of low-temperature multi-effect distillation seawater desalination system |
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