CN1473766A - Two-stage absorption compression high temperature heat pump seawater desalination device - Google Patents
Two-stage absorption compression high temperature heat pump seawater desalination device Download PDFInfo
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- CN1473766A CN1473766A CNA031169813A CN03116981A CN1473766A CN 1473766 A CN1473766 A CN 1473766A CN A031169813 A CNA031169813 A CN A031169813A CN 03116981 A CN03116981 A CN 03116981A CN 1473766 A CN1473766 A CN 1473766A
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- 239000013535 sea water Substances 0.000 title claims abstract description 69
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 24
- 238000010612 desalination reaction Methods 0.000 title claims description 14
- 230000006835 compression Effects 0.000 title claims description 11
- 238000007906 compression Methods 0.000 title claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000006096 absorbing agent Substances 0.000 claims abstract description 41
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims description 19
- 238000004062 sedimentation Methods 0.000 claims description 14
- 238000004821 distillation Methods 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000012808 vapor phase Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 8
- 238000001914 filtration Methods 0.000 abstract description 4
- 150000003839 salts Chemical class 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 239000003507 refrigerant Substances 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract 1
- 238000011033 desalting Methods 0.000 abstract 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 8
- 235000011114 ammonium hydroxide Nutrition 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
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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
Description
技术领域：Technical field:
本发明涉及的是一种海水淡化装置，特别是一种以海水为热源的双级吸收压缩式高温热泵海水淡化装置，属于机电、制冷及海水淡化技术领域。The invention relates to a seawater desalination device, in particular to a double-stage absorption compression high-temperature heat pump seawater desalination device using seawater as a heat source, belonging to the technical fields of electromechanical, refrigeration and seawater desalination.
背景技术：Background technique:
随着水资源的日益紧缺，海水淡化已经受到人们广泛的关注，现今的淡化方法一般需要大量的高温热源或电力供海水蒸馏，淡化成本较高。热泵系统作为一种逆向能源转换方式，能较好地利用低品位能源和余热，作为一种有效节能的方式已在采暖供热，干燥加工等领域中得到应用，效益十分明显。但是常规的压缩式热泵由于受到压缩比和排气压力的制约，提供的热源温度不宜高于50℃；而常规吸收式热泵本身就需要高温热源，而且吸收、发生过程中的传热传质阻力很大，效率低，也不能提供100℃以上的热源。With the increasing shortage of water resources, seawater desalination has attracted widespread attention. Today's desalination methods generally require a large amount of high-temperature heat source or electricity for seawater distillation, and the cost of desalination is relatively high. As a reverse energy conversion method, the heat pump system can make better use of low-grade energy and waste heat. As an effective energy-saving method, it has been applied in the fields of heating, drying and processing, and the benefits are very obvious. However, conventional compression heat pumps are limited by the compression ratio and exhaust pressure, so the temperature of the heat source provided should not be higher than 50°C; while the conventional absorption heat pump itself requires a high-temperature heat source, and the heat and mass transfer resistance in the process of absorption and generation It is very large, has low efficiency, and cannot provide a heat source above 100°C.
发明内容：Invention content:
为了克服已有技术的不足和缺陷，本发明综合压缩式热泵和吸收式热泵的优点，设计一种以海水为热源的双级吸收压缩式高温热泵海水淡化装置，能提供120℃以上的热源供海水淡化蒸馏过程应用。该装置利用压缩机的吸、排气作用强化吸收式系统中的吸收，发生过程，使系统更接近劳伦兹循环，因而具有较高的效率：同时装置采用氨作为制冷剂，既无温室效应，对环境也无任何破坏作用。本发明以海水为热源，可提供120℃以上温度的热源供海水蒸馏用，能效比可达3.5-4.0，极大地降低了海水淡化的成本。In order to overcome the deficiencies and defects of the prior art, the present invention integrates the advantages of compression heat pumps and absorption heat pumps, and designs a double-stage absorption compression high-temperature heat pump seawater desalination device with seawater as the heat source, which can provide heat supply above 120°C. Seawater desalination distillation process application. The device utilizes the suction and exhaust functions of the compressor to strengthen the absorption in the absorption system, and the process occurs, making the system closer to the Lorentz cycle, so it has higher efficiency: at the same time, the device uses ammonia as the refrigerant, which has no greenhouse effect , without any damage to the environment. The invention uses seawater as a heat source, can provide a heat source with a temperature above 120°C for seawater distillation, and has an energy efficiency ratio of up to 3.5-4.0, greatly reducing the cost of seawater desalination.
本发明的另一特点是该装置在吸收海水热量的同时使海水冷却，通过沉淀池的沉淀和过滤装置的过滤，可去除部分结晶盐和杂质，因而使海水蒸馏时的发生温度有所降低，进一步降低了能耗。Another feature of the present invention is that the device cools the seawater while absorbing the heat of the seawater, and can remove part of the crystallized salt and impurities through the sedimentation in the sedimentation tank and the filtration of the filter device, thereby reducing the occurrence temperature of the seawater distillation. Further reduce energy consumption.
本发明主要包括：低温发生器、低温汽液分离器、低温热交换器、氨压缩机、第一单向阀、发生吸收器、高温汽液分离器、高温热交换器、第二单向阀、高温吸收器、海水蒸馏器、凝结器、沉淀池、过滤池、调节阀以及泵等。The invention mainly includes: low-temperature generator, low-temperature vapor-liquid separator, low-temperature heat exchanger, ammonia compressor, first check valve, generator absorber, high-temperature vapor-liquid separator, high-temperature heat exchanger, second check valve , high temperature absorber, seawater distiller, condenser, sedimentation tank, filter tank, regulating valve and pump, etc.
本装置中的双级吸收压缩式热泵系统以海水为低温热源、吸收海水中的热量，通过热泵系统，得到120℃以上的高温热源，供海水蒸馏用。低温侧与高温侧两个独立的吸收式部分，通过氨压缩机和发生吸收器被串接起来。低温侧吸收式部分在低温发生器中吸收海水低温热源的热量，所产生的吸收热在发生吸收器中被传输给高温侧吸收式部分，使发生的气体在高温汽液分离器中分离后再次压缩，最后在高温吸收器中被吸收并产生大量的热量，使吸收器中的传热介质达到120℃以上，供海水蒸馏用。The two-stage absorption compression heat pump system in this device uses seawater as a low-temperature heat source to absorb heat in seawater, and through the heat pump system, obtains a high-temperature heat source above 120°C for seawater distillation. The low-temperature side and the high-temperature side are two independent absorption parts connected in series through an ammonia compressor and a generator absorber. The low-temperature side absorption part absorbs the heat of the seawater low-temperature heat source in the low-temperature generator, and the generated absorption heat is transferred to the high-temperature side absorption part in the generation absorber, so that the generated gas is separated in the high-temperature gas-liquid separator and then regenerated. Compressed, and finally absorbed in the high-temperature absorber to generate a large amount of heat, so that the heat transfer medium in the absorber reaches above 120°C for seawater distillation.
本发明综合压缩式热泵和吸收式热泵的优点，能提供120℃以上的热源供海水淡化蒸馏过程应用，能效比可达3.5-4.0，极大地降低了海水淡化的成本。该装置在吸收海水热量的同时使海水冷却，通过沉淀池的沉淀和过滤装置的过滤，可去除部分结晶盐和杂质，因而使海水蒸馏时的发生温度有所降低，进一步降低了能耗。The invention integrates the advantages of the compression heat pump and the absorption heat pump, can provide a heat source above 120°C for the seawater desalination distillation process, and has an energy efficiency ratio of 3.5-4.0, greatly reducing the cost of seawater desalination. The device cools the seawater while absorbing heat from the seawater, and removes part of the crystallized salt and impurities through sedimentation in the sedimentation tank and filtration by the filter device, thereby reducing the temperature of seawater distillation and further reducing energy consumption.
附图说明：Description of drawings:
图1是双级吸收压缩式高温热泵海水淡化装置的结构示意图。Fig. 1 is a structural schematic diagram of a double-stage absorption compression high temperature heat pump seawater desalination device.
图中1是低温发生器，2是低温汽液分离器，3是低温热交换器，4是氨压缩机，5是第一单向阀，6是发生吸收器，7是高温汽液分离器，8是高温热交换器，9是第二单向阀，10是高温吸收器，11是海水蒸馏器，12是凝结器，13是沉淀池，14是过滤池，15是海水泵，16是第一溶液泵，17是第二溶液泵，18是循环泵，19是调节阀。In the figure, 1 is a low-temperature generator, 2 is a low-temperature gas-liquid separator, 3 is a low-temperature heat exchanger, 4 is an ammonia compressor, 5 is the first one-way valve, 6 is a generator absorber, and 7 is a high-temperature gas-liquid separator , 8 is a high-temperature heat exchanger, 9 is a second one-way valve, 10 is a high-temperature absorber, 11 is a seawater distiller, 12 is a condenser, 13 is a sedimentation tank, 14 is a filter tank, 15 is a seawater pump, 16 is The first solution pump, 17 is the second solution pump, 18 is a circulation pump, and 19 is a regulating valve.
具体实施方式：Detailed ways:
下面结合附图对本发明的具体实施作进一步的描述。The specific implementation of the present invention will be further described below in conjunction with the accompanying drawings.
如图1所示本发明主要包括低温发生器1，低温汽液分离器2，低温热交换器3，氨压缩机4，第一单向阀5，发生吸收器6，高温汽液分离器7，高温热交换器8，第二单向阀9，高温吸收器10，海水蒸馏器11，凝结器12，沉淀池13，过滤池14，海水泵15，第一溶液泵16，第二溶液泵17，循环泵18、调节阀19等。As shown in Figure 1, the present invention mainly comprises low-temperature generator 1, low-temperature gas-liquid separator 2, low-temperature heat exchanger 3, ammonia compressor 4, first check valve 5, generating absorber 6, high-temperature gas-liquid separator 7 , high temperature heat exchanger 8, second one-way valve 9, high temperature absorber 10, seawater distiller 11, condenser 12, sedimentation tank 13, filter tank 14, seawater pump 15, first solution pump 16, second solution pump 17, circulation pump 18, regulating valve 19, etc.
低温发生器1的壳程进口和低温热交换器3的壳程出口连接，低温发生器1的管程进口和海水泵15的出口连接，低温发生器1的管程出口和沉淀池13的进口连接。低温汽液分离器2的汽相出口和氨压缩机4的吸气口连接，液相出口通过第一溶液泵16和低温热交换器3的管程进口连接。低温热交换器3的管程出口和发生吸收器6的壳程进口连接，低温热交换器3的壳程进口和发生吸收器6的壳程出口连接。氨压缩机4的吸气口还通过调节阀19和高温汽液分离器7的汽相出口连接，氨压缩机4的排气口分别通过第一单向阀5、第二单向阀9和发生吸收器6的壳程进口、高温吸收器10的壳程进口连接。发生吸收器6的管程进口和高温热交换器8的壳程出口连接，发生吸收器6的管程出口和高温汽液分离器7的进口连接。高温汽液分离器7的液相出口通过第二溶液泵17和高温热交换器8的管程进口连接。高温热交换器8的管程出口和高温吸收器10的壳程进口连接，高温热交换器8的壳程进口和高温吸收器10的壳程出口连接。高温吸收器10的管程进口和海水蒸馏器11的管程出口连接，高温吸收器10的管程出口通过循环泵18和海水蒸馏器11的管程进口连接。海水蒸馏器11的壳程进口和凝结器12的管程出口连接，海水蒸馏器11的蒸汽出口通到凝结器12的壳程进口。凝结器12的管程进口和过滤池14的海水出口连接，过滤池14的海水进口和沉淀池13的出口连接。海水泵15的进口和海水相通。The shell-side inlet of low-temperature generator 1 is connected to the shell-side outlet of low-temperature heat exchanger 3, the tube-side inlet of low-temperature generator 1 is connected to the outlet of seawater pump 15, and the tube-side outlet of low-temperature generator 1 is connected to the inlet of sedimentation tank 13 connect. The gas-phase outlet of the low-temperature gas-liquid separator 2 is connected to the suction port of the ammonia compressor 4 , and the liquid-phase outlet is connected to the tube-side inlet of the low-temperature heat exchanger 3 through the first solution pump 16 . The tube-side outlet of the low-temperature heat exchanger 3 is connected to the shell-side inlet of the generator-absorber 6 , and the shell-side inlet of the low-temperature heat exchanger 3 is connected to the shell-side outlet of the generator-absorber 6 . The suction port of the ammonia compressor 4 is also connected with the vapor phase outlet of the high-temperature vapor-liquid separator 7 through the regulating valve 19, and the exhaust port of the ammonia compressor 4 is respectively passed through the first one-way valve 5, the second one-way valve 9 and the The shell-side inlet of the generator absorber 6 and the shell-side inlet of the high-temperature absorber 10 are connected. The tube-side inlet of the generator-absorber 6 is connected to the shell-side outlet of the high-temperature heat exchanger 8 , and the tube-side outlet of the generator-absorber 6 is connected to the inlet of the high-temperature gas-liquid separator 7 . The liquid phase outlet of the high temperature vapor-liquid separator 7 is connected to the tube side inlet of the high temperature heat exchanger 8 through the second solution pump 17 . The tube-side outlet of the high-temperature heat exchanger 8 is connected to the shell-side inlet of the high-temperature absorber 10 , and the shell-side inlet of the high-temperature heat exchanger 8 is connected to the shell-side outlet of the high-temperature absorber 10 . The tube-side inlet of the high-temperature absorber 10 is connected to the tube-side outlet of the seawater distiller 11 , and the tube-side outlet of the high-temperature absorber 10 is connected to the tube-side inlet of the seawater distiller 11 through a circulating pump 18 . The shell-side inlet of the seawater distiller 11 is connected to the tube-side outlet of the condenser 12 , and the steam outlet of the seawater distiller 11 is connected to the shell-side inlet of the condenser 12 . The tube-side inlet of the condenser 12 is connected to the seawater outlet of the filter tank 14 , and the seawater inlet of the filter tank 14 is connected to the outlet of the sedimentation tank 13 . The inlet of seawater pump 15 communicates with seawater.
经过低温热交换器3壳程冷却后的浓氨溶液进入低温发生器1的壳程吸收海水的热量后，进入低温汽液分离器2被分离成氨蒸汽和稀氨溶液，氨蒸汽被压缩机4的吸气口吸入，稀氨溶液经过第一溶液泵16进入低温热交换器3的管程，吸热后进入发生吸收器6的壳程，吸收从压缩机4排气口排出的高温高压氨蒸汽后成为浓氨溶液，所产生的吸收热在发生吸收器6中被传递给高温侧吸收部分，然后回到低温热交换器3的壳程。同时，在发生吸收器6管程中的浓氨溶液吸收了低温吸收式部分在发生吸收器6中产生的吸收热后，被加热发生，然后进入第二汽液分离器7被分离成氨蒸汽和稀氨溶液，氨蒸汽通过调节阀19被氨压缩机4的吸气口吸入，稀氨溶液经过第二溶液泵17进入高温热交换器8的管程，冷却后进入高温吸收器10的壳程，吸收氨压缩机4排出的高温高压蒸汽成为浓氨溶液，所释放的吸收热被高温吸收器10管程中的传热介质吸收，使传热介质的温度升高到120℃以上后，经过循环泵18，进入海水蒸馏器11的管程，将从凝结器12来的、经过预热的海水蒸发成水蒸汽，放出热量后的介质又回到高温吸收器10的管程进口。The concentrated ammonia solution cooled by the shell side of the low-temperature heat exchanger 3 enters the shell side of the low-temperature generator 1 to absorb the heat of seawater, and then enters the low-temperature gas-liquid separator 2 to be separated into ammonia vapor and dilute ammonia solution, and the ammonia vapor is pumped by the compressor Inhaled through the suction port of 4, the dilute ammonia solution enters the tube side of the low-temperature heat exchanger 3 through the first solution pump 16, and enters the shell side of the generator absorber 6 after absorbing heat, absorbing the high temperature and high pressure discharged from the exhaust port of the compressor 4 After the ammonia vapor becomes a concentrated ammonia solution, the heat of absorption generated is transferred to the high-temperature side absorption part in the generating absorber 6, and then returns to the shell side of the low-temperature heat exchanger 3. At the same time, after the concentrated ammonia solution in the tube side of the generator-absorber 6 absorbs the absorption heat generated by the low-temperature absorption type part in the generator-absorber 6, it is heated to generate ammonia, and then enters the second vapor-liquid separator 7 to be separated into ammonia vapor and dilute ammonia solution, the ammonia vapor is sucked by the air inlet of the ammonia compressor 4 through the regulating valve 19, the dilute ammonia solution enters the tube side of the high-temperature heat exchanger 8 through the second solution pump 17, and enters the shell of the high-temperature absorber 10 after cooling In the process of absorbing ammonia, the high-temperature and high-pressure steam discharged from the compressor 4 becomes concentrated ammonia solution, and the released absorption heat is absorbed by the heat transfer medium in the high-temperature absorber 10, so that the temperature of the heat transfer medium rises above 120°C. Through the circulation pump 18, it enters the tube side of the seawater distiller 11, evaporates the preheated seawater from the condenser 12 into water vapor, and the medium after releasing heat returns to the tube side inlet of the high temperature absorber 10.
另一路是海水循环，海水泵15抽上来的海水在低温发生器1管程中放热冷却后进入沉淀池13沉淀和过滤装置14过滤后，被去除了部分结晶盐与杂质，然后经过凝结器12的管程，在其中被水蒸汽放出的凝结热预热后，进入海水蒸馏器11的壳程，在120℃以上的高温热源作用下被蒸发汽化，水蒸汽进入凝结器12放出热量后被凝结成淡水。The other way is seawater circulation. The seawater pumped up by the seawater pump 15 is exothermic and cooled in the tube side of the low-temperature generator 1, and then enters the sedimentation tank 13 for sedimentation and filtration by the filter device 14. Part of the crystallized salt and impurities are removed, and then passes through the condenser 12. The tube side, which is preheated by the condensation heat released by water vapor, enters the shell side of the seawater distiller 11, and is evaporated and vaporized under the action of a high-temperature heat source above 120°C, and the water vapor enters the condenser 12 to release heat and is condensed into freshwater.
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| CNB031169813A CN1194901C (en) | 2003-05-16 | 2003-05-16 | Double stage absorptive compressing type high temperature heat pump sea water desalination device |
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| CNB031169813A CN1194901C (en) | 2003-05-16 | 2003-05-16 | Double stage absorptive compressing type high temperature heat pump sea water desalination device |
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| CN1473766A true CN1473766A (en) | 2004-02-11 |
| CN1194901C CN1194901C (en) | 2005-03-30 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323032C (en) * | 2005-04-11 | 2007-06-27 | 国家海洋局天津海水淡化与综合利用研究所 | Apparatus of combined solar energy heat pump for desaltination of sea water |
| CN102166634A (en) * | 2011-04-12 | 2011-08-31 | 芜湖恒泰有色线材股份有限公司 | Cooling water recycling method for copper-bar crystallization cooling systems |
| CN102320675A (en) * | 2011-06-29 | 2012-01-18 | 中国科学院广州能源研究所 | Seawater desalting device and method |
| CN102910694A (en) * | 2012-10-31 | 2013-02-06 | 南京紫晶藤节能科技有限公司 | System and method for continuous production two-stage heat pump sea water desalinization |
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