CN201834781U - Single-stage vacuum distillation seawater desalination device - Google Patents
Single-stage vacuum distillation seawater desalination device Download PDFInfo
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- 239000013535 sea water Substances 0.000 title claims abstract description 140
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 29
- 238000005292 vacuum distillation Methods 0.000 title claims abstract description 9
- 239000013505 freshwater Substances 0.000 claims abstract description 109
- 239000002918 waste heat Substances 0.000 claims abstract description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 230000001105 regulatory effect Effects 0.000 claims abstract description 49
- 238000001704 evaporation Methods 0.000 claims abstract description 47
- 230000008020 evaporation Effects 0.000 claims abstract description 39
- 238000005086 pumping Methods 0.000 claims abstract description 33
- 239000011552 falling film Substances 0.000 claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 11
- 238000004821 distillation Methods 0.000 description 8
- 239000012267 brine Substances 0.000 description 6
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 6
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000502 dialysis Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 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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Abstract
一种单级真空蒸馏海水淡化装置，属于海水淡化技术领域。由加热器、蒸发室、蒸发管、除沫器、布水循环泵、布水装置、冷凝器、淡水槽、冷却器组成的降膜蒸馏器，以及淡水余热换热器、浓海水余热换热器、抽真空和抽淡水调节阀组成，布水循环泵连接在蒸发室的底部，补水流量调节阀与冷却器相连，并连接在布水循环泵与蒸发室的连接管路上，蒸发室通过一个浓海水排出流量调节阀与浓海水余热换热器相连排出浓海水，淡水槽通过抽真空和抽淡水调节阀与淡水余热换热器相连，新鲜海水通过淡水余热换热器和浓海水余热换热器进入冷却器。其优点是装置的结构简单，排出的浓海水流量和浓度可调节，排出的浓海水和淡水的温度低，装置节能高效、造水比高。
A single-stage vacuum distillation seawater desalination device belongs to the technical field of seawater desalination. Falling film distiller composed of heater, evaporating chamber, evaporating pipe, demister, water distribution circulation pump, water distribution device, condenser, fresh water tank, cooler, as well as fresh water waste heat exchanger and concentrated seawater waste heat exchanger , Vacuum pumping and fresh water regulating valves, the water distribution circulation pump is connected to the bottom of the evaporation chamber, the replenishment flow regulating valve is connected to the cooler, and connected to the connecting pipeline between the water distribution circulation pump and the evaporation chamber, and the evaporation chamber is discharged through a concentrated seawater The flow regulating valve is connected to the concentrated seawater waste heat exchanger to discharge the concentrated seawater. The fresh water tank is connected to the fresh water waste heat exchanger through the vacuum and fresh water regulating valve. The fresh seawater is cooled through the fresh water waste heat exchanger and the concentrated seawater waste heat exchanger. device. The advantage is that the structure of the device is simple, the flow rate and concentration of the discharged concentrated seawater can be adjusted, the temperature of the discharged concentrated seawater and fresh water is low, the device is energy-saving and efficient, and the water production ratio is high.
Description
(一)技术领域(1) Technical field
本实用新型涉及一种海水淡化装置，尤其涉及一种单级真空蒸馏海水淡化装置，主要用于海水(或苦咸水)淡化，属于海水淡化技术领域。The utility model relates to a seawater desalination device, in particular to a single-stage vacuum distillation seawater desalination device, which is mainly used for seawater (or brackish water) desalination and belongs to the technical field of seawater desalination.
(二)背景技术(2) Background technology
对海水或苦咸水进行淡化的方法很多，常规的方法有蒸馏法、离子交换法、渗析法、反渗透膜法以及冷冻法等。在蒸馏法中最为广泛被研究和使用的方法主要是多级闪蒸(MSF)海水淡化装置和多效蒸馏(MED)海水淡化装置。There are many methods for desalination of seawater or brackish water, conventional methods include distillation, ion exchange, dialysis, reverse osmosis membrane and freezing. The most widely studied and used methods in distillation are mainly multi-stage flash (MSF) seawater desalination unit and multi-effect distillation (MED) seawater desalination unit.
多级闪蒸(MSF)海水淡化装置是将原料海水加热到一定温度后引入闪蒸室，由于该闪蒸室中的压力控制在低于热盐水温度所对应的饱和蒸汽压的条件下，故热盐水进入闪蒸室后即成为过热水而急速地部分气化，从而使热盐水自身的温度降低，所产生的蒸汽冷凝后即为所需的淡水。多级闪蒸就是使热盐水依次流经若干个压力逐渐降低的闪蒸室，逐级蒸发降温，同时盐水也逐级增浓，直到其温度接近(但高于)天然海水温度。The multi-stage flash (MSF) seawater desalination device heats the raw seawater to a certain temperature and then introduces it into the flash chamber. Since the pressure in the flash chamber is controlled below the saturated vapor pressure corresponding to the temperature of the hot brine, the After the hot brine enters the flash chamber, it becomes superheated water and is rapidly partially vaporized, thereby reducing the temperature of the hot brine itself, and the generated steam is condensed to become the required fresh water. Multi-stage flash evaporation is to make hot brine flow through several flash chambers in which the pressure is gradually reduced, and the temperature of the brine is gradually reduced. At the same time, the brine is also gradually concentrated until its temperature is close to (but higher than) the natural seawater temperature.
多效蒸馏(MED)海水淡化技术的特征是将水平管降膜蒸发器(或垂直管降膜蒸发器)串联起来，用一定量的蒸汽输入，通过多次蒸发和冷凝，得到多倍于加热蒸汽量的蒸馏水。Multi-effect distillation (MED) seawater desalination technology is characterized by connecting horizontal tube falling film evaporators (or vertical tube falling film evaporators) in series, using a certain amount of steam input, through multiple evaporation and condensation, to obtain multiple times the heating steam volume of distilled water.
在上述两种方式海水淡化装置中，多级闪蒸海水淡化装置需要输入的蒸汽温度较高，温度过低导致级数减少，效率降低。由于多级闪蒸海水淡化装置每淡化1吨淡水需要8吨海水循环经过这个装置，因此必须需要大功率的循环水泵，其最大的缺点就是能耗高。而传统的多效蒸馏海水淡化装置在运行过程中，海水依次从上一效的蒸发室底部通过喷淋装置(或布水装置)进入到下一效，因此为了满足喷淋装置对海水流量的要求，海水流经各效的流量是不能随意调节的，流量过大和流量过小都会影响蒸发效率和蒸发器的寿命。因此，现有多效蒸馏海水淡化装置排出的浓海水的浓度都比较低(一般在5-6％左右)，这样的结果就是生产1吨淡水大约就要排出1吨浓海水。Among the above two types of seawater desalination devices, the multi-stage flash seawater desalination device needs to input steam at a higher temperature, and if the temperature is too low, the number of stages will be reduced and the efficiency will be reduced. Since the multi-stage flash seawater desalination device requires 8 tons of seawater to circulate through the device for desalination of 1 ton of fresh water, it must require a high-power circulating water pump, and its biggest disadvantage is high energy consumption. During the operation of the traditional multi-effect distillation seawater desalination device, the seawater enters the next effect from the bottom of the evaporation chamber of the previous effect through the spray device (or water distribution device), so in order to meet the requirements of the spray device for seawater flow It is required that the flow rate of seawater flowing through each effect cannot be adjusted arbitrarily. If the flow rate is too large or too small, it will affect the evaporation efficiency and the life of the evaporator. Therefore, the concentration of the concentrated seawater discharged from the existing multi-effect distillation seawater desalination device is relatively low (generally about 5-6%), and such a result is to produce 1 ton of fresh water and approximately will discharge 1 ton of concentrated seawater.
传统理论认为增加级数可以提高造水比，因此，现有海水淡化装置一般是通过增加级数(或效数)作为提高造水比的主要手段，现有的多级闪蒸海水淡化装置的级数多达30级，而多效蒸馏海水淡化装置一般在6至10级，甚至高达十几级。然而从能量守恒定律对真空蒸馏海水淡化装置造水比的分析表明，造水比与级数(效数)无关。计算分析如下：The traditional theory believes that increasing the number of stages can increase the water production ratio. Therefore, the existing seawater desalination devices generally use increasing the number of stages (or effect numbers) as the main means to increase the water production ratio. The existing multi-stage flash seawater desalination device The number of stages is as many as 30, while the multi-effect distillation seawater desalination device is generally in the range of 6 to 10, or even as high as a dozen. However, the analysis of the water production ratio of the vacuum distillation seawater desalination device from the law of energy conservation shows that the water production ratio has nothing to do with the number of stages (effectiveness). The calculation and analysis are as follows:
假设1吨/h蒸汽产生的淡水为X吨/h淡水(即造水比为X)，假设淡水与浓海水的比值为K，则排出的浓海水为1/K＊X吨/h，流进海水淡化装置的海水为(X+1/K＊X)吨/h。假设海水温度25℃，排出的浓海水和淡水的温度为t℃，汽化潜热取2200KJ/Kg；根据热力学第一定律(即能量守恒定律)，装置稳定运行时，输入的热量与排出的热量相等，即：Assuming that the fresh water produced by 1 ton/h steam is X tons/h fresh water (that is, the water production ratio is X), assuming that the ratio of fresh water to concentrated seawater is K, then the discharged concentrated seawater is 1/K*X tons/h, flow The seawater entering the seawater desalination device is (X+1/K*X) tons/h. Assuming that the seawater temperature is 25°C, the temperature of the discharged concentrated seawater and fresh water is t°C, and the latent heat of vaporization is 2200KJ/Kg; according to the first law of thermodynamics (that is, the law of energy conservation), when the device operates stably, the heat input is equal to the heat discharged ,Right now:
1×1000Kg×2200KJ/Kg＝(X+1/K＊X)×1000Kg×(t-25)×4.2KJ/Kg1×1000Kg×2200KJ/Kg＝(X+1/K*X)×1000Kg×(t-25)×4.2KJ/Kg
求得：X＝524K/(K+1)(t-25)。假设K为1(浓缩1倍)，排出的淡水和浓海水温度为45℃，则造水比约为13，这就是现代多效蒸馏海水淡化装置的理论造水比(实际为10)。如果K为3(即海水浓缩4倍)，排出的浓海水和淡水温度为45℃，则造水比为19，若排出浓海水和淡水的温度降低到35℃，理论造水比为39。Obtain: X=524K/(K+1)(t-25). Assuming that K is 1 (concentrated twice), and the temperature of the discharged fresh water and concentrated seawater is 45°C, the water production ratio is about 13, which is the theoretical water production ratio of modern multi-effect distillation seawater desalination devices (actually 10). If K is 3 (that is, the concentration of seawater is 4 times), and the temperature of the discharged concentrated seawater and fresh water is 45°C, the water generation ratio is 19. If the temperature of the discharged concentrated seawater and fresh water is reduced to 35°C, the theoretical water generation ratio is 39.
由此可见，造水比主要和浓缩率以及排出淡水和浓海水的温度有关，而与级数无关。即使采用一级真空蒸馏，只要尽可能提高浓缩率和降低排出淡水和浓海水的温度，同样可以达到极高的造水比。It can be seen that the water production ratio is mainly related to the concentration rate and the temperature of the discharged fresh water and concentrated sea water, but has nothing to do with the number of stages. Even if one-stage vacuum distillation is adopted, as long as the concentration rate is increased as much as possible and the temperature of discharged fresh water and concentrated seawater is lowered, a very high water production ratio can also be achieved.
(三)发明内容(3) Contents of the invention
为了克服上述两种海水淡化装置的缺点，本实用新型提供了一种带有流量调节装置和排出淡水和浓海水余热回收的单级真空蒸馏海水淡化装置，其排出的淡水和浓海水的温度低、浓度可调节，因而具有造水比高、节能高效的优点。In order to overcome the shortcomings of the above two seawater desalination devices, the utility model provides a single-stage vacuum distillation seawater desalination device with a flow regulating device and waste heat recovery of discharged fresh water and concentrated seawater. The temperature of the discharged fresh water and concentrated seawater is low. , The concentration can be adjusted, so it has the advantages of high water production ratio, energy saving and high efficiency.
本实用新型是这样实现的：The utility model is achieved in that:
方案一：Option One:
由加热器、蒸发室、除沫器、冷凝器、淡水槽、冷却器组成的浸没式真空蒸馏器，以及淡水余热换热器、浓海水余热换热器、抽真空和抽淡水调节阀组成。蒸发室通过一个补水流量调节阀与冷却器相连，蒸发室通过一个浓海水排出流量调节阀与浓海水余热换热器相连排出浓海水，淡水槽通过抽真空和抽淡水调节阀与淡水余热换热器相连，再连接到抽真空、抽淡水装置，新鲜海水通过淡水余热换热器和浓海水余热换热器进入冷却器。Submerged vacuum distiller composed of heater, evaporation chamber, demister, condenser, fresh water tank, cooler, fresh water waste heat exchanger, concentrated seawater waste heat exchanger, vacuum pumping and fresh water pumping regulating valve. The evaporating chamber is connected to the cooler through a water supply flow regulating valve, the evaporating chamber is connected to the concentrated seawater waste heat exchanger through a concentrated seawater discharge flow regulating valve to discharge concentrated seawater, and the fresh water tank exchanges heat with the fresh water waste heat through vacuuming and fresh water regulating valve Connected to the device, and then connected to the vacuum pumping and fresh water pumping device, fresh seawater enters the cooler through the fresh water waste heat exchanger and the concentrated seawater waste heat heat exchanger.
方案二：Option II:
由加热器、蒸发室、蒸发管、除沫器、布水循环泵、布水装置、冷凝器、淡水槽、冷却器组成的降膜蒸馏器，以及淡水余热换热器、浓海水余热换热器、抽真空和抽淡水调节阀组成。布水循环泵连接在蒸发室的底部，补水流量调节阀与冷却器相连，并连接在布水循环泵与蒸发室的连接管路上，蒸发室通过一个浓海水排出流量调节阀与浓海水余热换热器相连排出浓海水，淡水槽通过抽真空和抽淡水调节阀与淡水余热换热器相连，再连接到抽真空、抽淡水装置，新鲜海水通过淡水余热换热器和浓海水余热换热器进入冷却器。Falling film distiller composed of heater, evaporating chamber, evaporating pipe, demister, water distribution circulation pump, water distribution device, condenser, fresh water tank, cooler, as well as fresh water waste heat exchanger and concentrated seawater waste heat exchanger , Vacuum pumping and pumping fresh water regulating valve. The water distribution circulation pump is connected to the bottom of the evaporation chamber, the replenishment flow regulating valve is connected to the cooler, and connected to the connecting pipeline between the water distribution circulation pump and the evaporation chamber, and the evaporation chamber passes through a concentrated seawater discharge flow regulating valve and a concentrated seawater waste heat exchanger Concentrated seawater is discharged in a row, and the fresh water tank is connected to the fresh water waste heat exchanger through the vacuum pumping and fresh water regulating valve, and then connected to the vacuum pumping and fresh water pumping device. device.
(四)附图说明(4) Description of drawings
图1是本实用新型的一个实施例。Fig. 1 is an embodiment of the present utility model.
图2是本实用新型的另一个实施例。Fig. 2 is another embodiment of the utility model.
图中1：1是加热器、2除沫器、3蒸发室、4浓海水流量调节阀、5补水流量调节阀、6冷凝器、7淡水槽、8冷却器、9抽真空和抽淡水调节阀、10浓海水余热换热器、11、淡水余热换热器。1:1 in the figure is the heater, 2 demister, 3 evaporation chamber, 4 concentrated seawater flow regulating valve, 5 make-up water flow regulating valve, 6 condenser, 7 fresh water tank, 8 cooler, 9 vacuum and fresh water adjustment Valve, 10 thick seawater waste heat exchanger, 11, fresh water waste heat exchanger.
图中2：1是加热器、2蒸发室、3布水装置、4除沫器、5蒸发管、6布水循环泵、7浓海水流量调节阀、8补水流量调节阀、9冷凝器、10冷却器、11淡水槽、12抽真空和抽淡水调节阀、13浓海水余热换热器、14淡水余热换热器。2 in the figure: 1 is the heater, 2 evaporation chamber, 3 water distribution device, 4 demister, 5 evaporation pipe, 6 water distribution circulation pump, 7 concentrated seawater flow regulating valve, 8 replenishing water flow regulating valve, 9 condenser, 10 Cooler, 11 fresh water tank, 12 vacuum and fresh water regulating valve, 13 concentrated seawater waste heat exchanger, 14 fresh water waste heat exchanger.
(五)具体实施方式(5) Specific implementation methods
图1是基于浸没式蒸馏器的一个实施例。Figure 1 is an embodiment based on a submerged still.
热源从A、B口进入到加热器1中，热量通过加热管(或加热板)的外表面加热蒸发室3中的海水，抽真空和抽淡水装置连接到b口，抽真空和抽淡水装置通过淡水余热换热器11，再经过抽真空和抽淡水调节阀8连接到淡水槽7，冷凝器6的顶部通过管路连接到蒸发室3的顶部，通过调节抽真空和抽淡水调节阀9的开度，可以调节真空蒸馏器中的真空度，以及把淡水从淡水槽7中抽出。当加热器1将蒸发室3中的海水加热到真空下所对应的沸点时海水沸腾，蒸汽经过除沫器2通过管路进入到冷凝器6中凝结成淡水，淡水流入淡水槽7中，而蒸汽凝结释放的凝结热被冷却器8中的海水吸收。蒸发室3和冷却器之间连接有补水流量调节阀5，冷却器中的海水经过流量调节阀5为蒸发室补充海水，通过调节补水流量调节阀5可以调节补水流量，从而保证蒸发室3的海水保持适当的高度，确保蒸发器正常工作。淡水槽中的淡水经过抽真空和抽淡水调节阀9和淡水余热换热器11，被淡水余热换热器中的新鲜海水冷却后由抽真空和抽淡水装置从b口排出。蒸发室3底部连接有排出浓海水流量调节阀4，通过调节浓海水流量调节阀4的开度可以控制排出浓海水的流量，从而控制蒸发室中海水的浓度，排出浓海水的流量越大，排出浓海水的浓度越低，流量越小浓度越高。浓海水经过浓海水余热换热器10被从淡水余热换热器出来的海水冷却后，由抽排浓海水的装置从a口排出，而新鲜海水从c口进入淡水余热换热器11加热后，再进入浓海水余热换热器10，被加热的海水进入到冷却器8中为其补充海水。The heat source enters the
上述装置中，调节浓海水流量调节阀4可以连接在浓海水余热换热器10的前面，也可以连接在浓海水余热换热器10的后边；抽真空和抽淡水调节阀9可以安装在淡水余热换热器11的前边，也可以安装在淡水余热换热器11的后边；浓海水余热换热器10和淡水余热换热器11也可以交换位置。In the above device, the regulating
图2是基于竖管降膜蒸馏器的另一个实施例。Figure 2 is another embodiment based on a standpipe falling film still.
热源从A、B口进入到加热器1中，热量通过加热管的内表面加热蒸发管5中的海水，抽真空和抽淡水装置连接到b口，抽真空和抽淡水装置通过淡水余热换热器14，再经过抽真空和抽淡水调节阀12连接到淡水槽11，冷凝器9的顶部通过管路连接到蒸发室2的顶部，通过调节抽真空和抽淡水调节阀12的开度，可以调节真空蒸馏器中的真空度，以及把淡水从淡水槽11中抽出。蒸发室2的底部安装有布水循环泵6，循环泵6把蒸发室2底部的海水连续不断的打入布水装置3中，布水装置3把海水均匀分布到蒸发管5的内表面，形成稳定的降膜。当加热器1将蒸发管5中的海水膜加热到真空下所对应的沸点时沸腾产生蒸汽，蒸汽经过除沫器4通过管路进入到冷凝器9中凝结成淡水，淡水流入淡水槽11中，而蒸汽凝结释放的凝结热被冷却器10中的海水吸收。淡水槽11中的淡水经过抽真空和抽淡水调节阀12进入到淡水余热换热器14，淡水被淡水余热换热器14中的新鲜海水冷却后由抽真空和抽淡水装置从b口排出。冷却器10上连接有补水流量调节阀8，补水流量调节阀8连接到布水循环泵6和蒸发室2之间的管路上，从冷却器补充过来的海水，直接进入到布水循环泵6中被打入到布水装置3中，通过调节补水流量调节阀8可以调节补水流量，从而保证蒸发室2中的海水保持适当的高度，确保蒸发器正常工作。蒸发室2底部连接有排出浓海水流量调节阀7，通过调节浓海水流量调节阀7的开度可以控制排出浓海水的流量，从而控制蒸发室中海水的浓度，排出浓海水的流量越大，排出浓海水的浓度越低，流量越小浓度越高。浓海水经过浓海水余热换热器13被从淡水余热换热器出来的海水冷却后，由抽排浓海水的装置从a口排出，而新鲜海水从c口进入淡水余热换热器14加热后，再进入浓海水余热换热器13，被加热的海水进入到冷却器10中为其补充海水。The heat source enters the
上述装置中，调节浓海水流量调节阀7可以连接在浓海水余热换热器13的前边，也可以连接在浓海水余热换热器13的后边；抽真空和抽淡水调节阀12可以安装在淡水余热换热器14的前边，也可以安装在淡水余热换热器14的后边；浓海水余热换热器13和淡水余热换热器14也可以交换位置。In the above device, the regulating
上述装置中采用的是竖管降膜蒸发器，也可以采用水平管降膜蒸发器，或者板式降膜蒸发器。The above-mentioned device adopts a vertical tube falling film evaporator, and a horizontal tube falling film evaporator or a plate type falling film evaporator can also be used.
在上述两个实施例中，淡水余热换热器和浓海水余热换热器也可以串联在冷却器和蒸发室之间的由补水流量调节阀组成的补水管路上，新鲜海水可以直接进入冷却器内，或者再通过第二组浓海水余热换热器和淡水余热换热器进入冷却器。In the above two embodiments, the fresh water waste heat exchanger and the concentrated seawater waste heat exchanger can also be connected in series on the make-up water pipeline composed of a make-up water flow regulating valve between the cooler and the evaporation chamber, and fresh seawater can directly enter the cooler or enter the cooler through the second set of concentrated seawater waste heat exchangers and fresh water waste heat exchangers.
在上述两个实施例中，加热器(1)的热源可以是化工厂或电厂的余热，也可以是太阳能系统产生的热水，在特殊情况下也可以直接用电、煤或天然气加热。In the above two embodiments, the heat source of the heater (1) can be waste heat from a chemical plant or a power plant, or hot water produced by a solar system, or directly heated by electricity, coal or natural gas in special cases.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285702A (en) * | 2011-05-31 | 2011-12-21 | 于庆坤 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN102659194A (en) * | 2012-04-01 | 2012-09-12 | 傅利江 | Distillation-type seawater desalinization device |
| CN103145207A (en) * | 2013-03-19 | 2013-06-12 | 上海海事大学 | Sea water desalting device for twin-stage recovery of flue gas waste heat of marine steam turbine |
| CN103253722A (en) * | 2013-06-07 | 2013-08-21 | 浙江大学 | Plate type low-temperature multieffect seawater desalting device and method |
| CN104284881A (en) * | 2012-03-29 | 2015-01-14 | Htc普尔埃尼基公司 | System and process for reclaiming single and mixed amine solvents |
| CN109775789A (en) * | 2019-03-18 | 2019-05-21 | 齐鲁工业大学 | A heat pipe vacuum drying system and its application |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285702A (en) * | 2011-05-31 | 2011-12-21 | 于庆坤 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN102285702B (en) * | 2011-05-31 | 2014-07-16 | 烟台豪杰能源科技有限公司 | Device for seawater desalination by recovering waste heat from diesel engine with series-connected heat pipe heat exchangers |
| CN104284881A (en) * | 2012-03-29 | 2015-01-14 | Htc普尔埃尼基公司 | System and process for reclaiming single and mixed amine solvents |
| CN104284881B (en) * | 2012-03-29 | 2017-08-15 | Htc普尔埃尼基公司 | Reclaim single or mixing amine solvent system and method |
| US9994512B2 (en) | 2012-03-29 | 2018-06-12 | Htc Purenergy Inc. | System and process for reclaiming single and mixed amine solvents |
| CN102659194A (en) * | 2012-04-01 | 2012-09-12 | 傅利江 | Distillation-type seawater desalinization device |
| CN103145207A (en) * | 2013-03-19 | 2013-06-12 | 上海海事大学 | Sea water desalting device for twin-stage recovery of flue gas waste heat of marine steam turbine |
| CN103145207B (en) * | 2013-03-19 | 2014-04-09 | 上海海事大学 | Sea water desalting device for twin-stage recovery of flue gas waste heat of marine steam turbine |
| CN103253722A (en) * | 2013-06-07 | 2013-08-21 | 浙江大学 | Plate type low-temperature multieffect seawater desalting device and method |
| CN109775789A (en) * | 2019-03-18 | 2019-05-21 | 齐鲁工业大学 | A heat pipe vacuum drying system and its application |
| CN109775789B (en) * | 2019-03-18 | 2022-06-21 | 齐鲁工业大学 | Heat pipe vacuum drying system and application thereof |
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