CN108046361B - High-concentration distillation desalination system and method based on induced crystallization method - Google Patents
High-concentration distillation desalination system and method based on induced crystallization method Download PDFInfo
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- CN108046361B CN108046361B CN201711432917.9A CN201711432917A CN108046361B CN 108046361 B CN108046361 B CN 108046361B CN 201711432917 A CN201711432917 A CN 201711432917A CN 108046361 B CN108046361 B CN 108046361B
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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
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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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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
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- C02F2201/007—Modular design
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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
- C02F2303/00—Specific treatment goals
- C02F2303/22—Eliminating or preventing deposits, scale removal, scale prevention
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Abstract
The invention discloses a high-concentration distillation desalination system and a high-concentration distillation desalination method based on an induced crystallization method. When the device is started, the induction seed crystal which is the same as or similar to the scale crystal nucleus is added into the seawater through the seed crystal tank in advance, so that the crystallization scale formed in the evaporation process is preferentially attached to the surface of the induction seed crystal, the deposition on the heat exchange surface is blocked, a stock solution containing the induction crystal particles flows back to the forced circulation pipeline through the cyclone and the stock solution tank after normal operation, and is conveyed to each effect evaporator through the forced circulation pump to serve as the effect of the induction seed crystal without continuously adding the induction seed crystal. The method of the invention does not need to add chemical scale inhibitor in the whole process, can thoroughly eliminate the additional influence of the chemical scale inhibitor on the environment, can realize high-power concentration, and can greatly reduce the water intake of the raw material seawater and reduce the power consumption of the system operation on the premise of determining the water production load.
Description
Technical Field
The invention relates to the technical field of distillation seawater desalination, in particular to a high-concentration distillation desalination system and a seawater desalination method based on an induced crystallization method.
Background
The development and utilization of seawater resources and the development of seawater desalination technology are energetically important approaches to solve water resource crisis, and seawater desalination has become a major strategic measure for solving the shortage of fresh water resources and promoting the sustainable development of economic society in many countries. The seawater desalination technologies applied industrially so far mainly include two methods, distillation and reverse osmosis. Since seawater is a complex system and contains a large amount of salts, wherein the hardness of the salts is high due to carbonate, bicarbonate, sulfate, chloride and the like formed by a large amount of calcium and magnesium ions, particularly the salts such as calcium sulfate, calcium carbonate, magnesium hydroxide and the like have inverse solubility characteristics, and the solubility is lower at higher temperature. In the distillation desalination process, with the increase of the concentration multiple and the operation temperature, the inorganic salts with inverse solubility are easy to crystallize and separate out and deposit on the surface of the heat transfer pipe, thereby causing the surface of the heat transfer pipe to be scaled.
The concentration multiple is one of the important operation process parameters of the hot method seawater desalination system. On the premise that design conditions such as water yield of the system, quality of raw seawater and the like are determined, the higher the concentration times in the evaporation process is, the less the total water intake of the system is, the lower the power consumption of the fluid delivery pump is, and meanwhile, the concentration of the discharged strong brine is correspondingly increased, so that the scaling tendency of the system is increased. Research and development of high-efficiency scale inhibition technology and process, and improvement of system evaporation concentration ratio are important research directions in the field of hot seawater desalination.
In countries such as the United states, Saudi, Japan, Israel and the like where salt manufacturing industries are more developed or where seawater desalination technologies are applied earlier, numerous scholars have conducted targeted research on the scaling problem of heat transfer tubes in the process of concentrating multi-effect distilled seawater, and developed a scale inhibition method based on softening pretreatment (removal of hardness ions such as calcium and magnesium in advance), acidification and addition of a scale inhibitor, thereby greatly promoting the technical progress of the hot seawater desalination process.
Although the addition of the chemical scale inhibitor into the evaporation raw material seawater can delay the scaling rate of a heat transfer pipe in the multi-effect distillation desalination device, the scale inhibitor popularized and applied at the present stage enables the concentration rate in the distillation desalination process to hardly exceed 3, and is generally controlled to be 1.5-3. If the concentration ratio exceeds the control point, the chemical scale inhibitor is difficult to prevent the deposition of inorganic salt with inverse solubility on the surface of a heat transfer pipe to form dirt.
In addition, chemical scale inhibitors added into the evaporation raw material seawater need a medicament adding device for the multi-effect distillation seawater desalination system, so that the initial investment of equipment is increased to a certain extent, and on the other hand, the medicament consumption is high, so that the operation cost of the system is increased. In the distillation desalination process, chemical agents cannot be fully utilized and decomposed, a part of chemical agents enters the strong brine to influence the discharge quality of the strong brine, and the chemical scale inhibitor is sensitive to the environment and easily causes secondary pollution.
The analysis shows that although the scale deposition rate is slowed down to a certain extent by the chemical agent method scale deposition technology commonly adopted in the current commercial thermal desalination engineering, the defects of low concentration rate of the system, high operation cost, easy additional influence on the environment and the like still exist.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a high-concentration distillation desalination system based on an induced crystallization method.
The second purpose of the invention is to provide a high-concentration distillation desalination method based on an induced crystallization method.
The technical scheme of the invention is summarized as follows:
a high power concentration distillation desalination system based on induced crystallization method, raw material sea water charge pump 9 is connected with condenser 4 through the pipeline, the condenser is connected with cooling water discharge pump 12 through the cooling water pipeline, connect with feed valve 18 again and then connect with n evaporators, n is 1-7, preferably 3, the strong brine outlet of n evaporators connects with the inlet of the forced circulation pump 10 through the strong brine pipeline separately, the outlet of the forced circulation pump 10 divides into two routes, one route connects with outlet port of the feed valve 18, another route connects with strong brine discharge valve 14, inlet port of the swirler 6 sequentially; the bottom of the cyclone 6 is connected with a liquid discharge valve 15 through a pipeline and then is connected with a mother liquor tank 7, and the seed crystal tank 8 is connected with a seed crystal control valve 16, the mother liquor tank 7 and a reflux valve 17 in sequence through pipelines and then is connected with an inlet of a forced circulation pump 10; the first effect evaporator 1 is provided with a power steam inlet 20 and a first effect condensate water discharge port 21, the first effect evaporator is sequentially connected with the next-stage evaporator through a secondary steam pipeline, the last effect evaporator 3 is connected with the condenser 4 through a secondary steam pipeline, the last effect evaporator and the condenser are connected with the product water tank 5 through a product water pipeline and then are connected with the product water pump 11, and the top of each effect evaporator, the upper part of the condenser 4 and the top of the product water tank 5 are respectively connected with the noncondensable air control valve 19 through pipelines and then are connected with the vacuum pump 13.
A stirring device is arranged in the mother liquor tank 7.
A high-concentration distillation desalination method based on an induced crystallization method comprises the following steps:
1) the high-concentration distillation desalination system based on the induced crystallization method is used;
2) opening a raw material seawater feeding pump 9, a feeding valve 18, a forced circulation pump 10, a strong brine discharge valve 14, a liquid discharge valve 15, a cooling water discharge pump 12, a vacuum pump 13 and a noncondensable control valve 19, and introducing power steam into the first-effect evaporator 1 through a power steam inlet 20;
3) opening a seed crystal control valve 16, and introducing the induced seed crystal in the seed crystal tank 8 into the mother liquor tank 7;
4) raw seawater is sent into a condenser 4 for preheating through a raw seawater feeding pump 9;
5) one part of the preheated raw material seawater is discharged through a cooling water discharge pump 12, and the other part of the preheated raw material seawater is used as supplementary feed liquid seawater and enters n evaporators for evaporation through the flow regulation of a feed valve 18;
6) with the continuous input of power steam, the evaporation capacity of each effect evaporator is continuously increased, the water yield of the system is gradually increased, after the product water tank 5 reaches a specified liquid level, the product water pump 11 is started, the system enters a stable operation state after the water yield reaches a designed value, and the seed crystal control valve 16 is closed;
7) the power steam entering the first-effect evaporator 1 exchanges heat with the feed seawater and then is discharged from a first-effect condensate water discharge port 21, the secondary steam generated by each first-effect evaporator is introduced into the next effect for recycling, and the secondary steam generated by the last-effect evaporator is introduced into a condenser for recycling; product water generated by condensing the evaporators except the first-effect evaporator and the condenser 4 by steam enters a product water tank 5 and is discharged by a product water pump 11;
8) the strong brine remained by evaporation of each effect evaporator is mixed with the reflux mother liquor from the mother liquor tank 7 controlled by the reflux valve 17, and then is divided into two strands under the action of the forced circulation pump 10, one strand is mixed with the seawater flowing out through the feed valve 18, and enters each effect evaporator again for evaporation, and the other strand is introduced into the swirler 6 after being regulated by the strong brine discharge valve 14;
9) after the strong brine containing the scale crystals enters the cyclone 6, coarse particles move to the bottom of the cyclone under the centrifugal separation action of the cyclone 6, crystallization mother liquor deposited at the bottom of the cyclone 6 is discharged into a mother liquor tank 7 under the flow control of a liquid discharge valve 15, and supernate of the cyclone is discharged as the strong brine;
10) the inside of each effect evaporator and the condenser 4, as well as the product water tank 5, are maintained in a negative pressure state under the action of the vacuum pump 13, and the operating temperature of each effect evaporator is adjusted within the range of 50-100 ℃.
Preferably, the induction seeds are gypsum particles or calcite particles, but also other common induction seeds.
The grain size of the induction seed crystal is less than or equal to 300 mu m.
The invention has the advantages that:
in the system, during the evaporation process of seawater, scale crystal nuclei such as calcium sulfate and the like separated out by crystallization are preferentially attached to the surface of the induction seed crystal which is added in advance, so that the scale crystal deposition on the surface of the heat exchange tube to form scale is effectively reduced, the whole process flow does not need to add a chemical scale inhibitor, the additional influence of the chemical scale inhibitor on the environment can be thoroughly eliminated, and the medicament consumption cost of the system can be greatly reduced.
The system of the invention is insensitive to the salinity change of the raw material seawater, has stronger adaptability to the raw material liquid, and can greatly reduce the water intake of the raw material seawater on the premise of determining the water production load due to the high concentration multiple of the system, thereby reducing the power consumption of the system in operation.
The system of the invention can operate in the temperature range of 50-100 ℃, can realize high temperature evaporation above 90 ℃, has high heat transfer coefficient of the heat transfer pipe under the condition of higher evaporation temperature, and can design and adopt more effect numbers to improve the water making ratio.
Drawings
FIG. 1 is a schematic diagram of a high-concentration distillation desalination system based on an induced crystallization method.
Detailed Description
The system of the present invention is further described below with reference to the accompanying drawings.
A high power concentration distillation desalination system based on induced crystallization method, see figure 1, take number n of evaporators as 3 as an example, raw material sea water charge pump 9 is connected with condenser 4 through the pipeline, the condenser is connected with the discharge pump 12 of cooling water through the cooling water pipeline, connect with feed valve 18 and then connect with 3 evaporators, 3 evaporator strong brine exports are connected with the inlet of the forced circulation pump 10 through the strong brine pipeline respectively, the outlet of the forced circulation pump 10 divides into two routes, one route is connected with outlet port of the feed valve 18, another route is connected with the inlet of the strong brine discharge valve 14, swirler 6 sequentially; the bottom of the cyclone 6 is connected with a liquid discharge valve 15 through a pipeline and then is connected with a mother liquor tank 7, and the seed crystal tank 8 is connected with a seed crystal control valve 16, the mother liquor tank 7 and a reflux valve 17 in sequence through pipelines and then is connected with an inlet of a forced circulation pump 10; first effect evaporator 1 is provided with power steam inlet 20 and first effect comdenstion water discharge port 21, first effect evaporator passes through the secondary steam pipeline and in proper order with second effect evaporator 2, last effect evaporator 3 is connected, last effect evaporator 3 passes through the secondary steam pipeline and is connected with condenser 4, from second effect evaporator 2 to last effect evaporator 3 and condenser 4 pass through product water pipeline and be connected with product water pump 11 after being connected with product water tank 5, the top of each effect evaporator, the upper portion of condenser 4 and the top of product water tank 5 are connected with noncondensation air control valve 19 through the pipeline respectively and are connected with vacuum pump 13 again.
A stirring device is arranged in the mother liquor tank 7.
The number of the evaporators can also be 1, 2, 4, 5, 6 and 7.
The process of the present invention is further illustrated below with reference to specific examples.
Example 1
A high-concentration distillation desalination method based on an induced crystallization method comprises the following steps:
1) the high-concentration distillation desalination system based on the induced crystallization method is used, wherein 3 evaporators are taken as examples;
2) opening a raw material seawater feeding pump 9, a feeding valve 18, a forced circulation pump 10, a strong brine discharge valve 14, a liquid discharge valve 15, a cooling water discharge pump 12, a vacuum pump 13 and a noncondensable control valve 19, and introducing power steam into the first-effect evaporator 1 through a power steam inlet 20;
3) opening a seed crystal control valve 16, introducing the induced seed crystals in the seed crystal tank 8 into the mother liquor tank 7, wherein the mother liquor tank 7 is provided with a stirring device, so that the induced seed crystals in the tank are always in a suspension state;
4) raw seawater is sent into a condenser 4 for preheating through a raw seawater feeding pump 9;
5) one part of the preheated raw material seawater is discharged through a cooling water discharge pump 12, and the other part of the preheated raw material seawater is used as supplementary feed liquid seawater and enters 3 evaporators for evaporation through the flow regulation of a feed valve 18;
6) with the continuous input of power steam, the evaporation capacity of each effect evaporator is continuously increased, the water yield of the system is gradually increased, after the product water tank 5 reaches a specified liquid level, the product water pump 11 is started, the system enters a stable operation state after the water yield reaches a designed value, and the seed crystal control valve 16 is closed;
7) the power steam entering the first-effect evaporator 1 exchanges heat with the feed seawater and then is discharged from a first-effect condensate water discharge port 21, the secondary steam generated by each first-effect evaporator is introduced into the next effect for recycling, and the secondary steam generated by the last-effect evaporator is introduced into a condenser for recycling; product water generated by condensing the evaporators except the first-effect evaporator and the condenser 4 by steam enters a product water tank 5 and is discharged by a product water pump 11;
8) the strong brine remained by evaporation of each effect evaporator is mixed with the reflux mother liquor from the mother liquor tank 7 controlled by the reflux valve 17, and then is divided into two strands under the action of the forced circulation pump 10, one strand is mixed with the seawater flowing out through the feed valve 18, and enters each effect evaporator again for evaporation, and the other strand is introduced into the swirler 6 after being regulated by the strong brine discharge valve 14;
9) after the strong brine containing scale crystals enters the cyclone 6, coarse particles move towards the bottom of the cyclone under the centrifugal separation action of the cyclone 6, crystallization mother liquor deposited at the bottom of the cyclone 6 is discharged into a mother liquor tank 7 through the flow control of a liquid discharge valve 15, supernatant of the cyclone is discharged as the strong brine, and the detected strong brine has the concentration of 20 percent (more than 20 percent) and the evaporation concentration ratio of more than 5;
10) the inside of each effect evaporator and the condenser 4, as well as the product water tank 5, are maintained in a negative pressure state by the vacuum pump 13, and the operating temperature of each effect evaporator can be adjusted within the range of 50-100 ℃.
The inducing seed crystal adopted in the embodiment is gypsum particles with the particle size of less than or equal to 300 microns. Calcite particles can also be used as the induction seed crystals, and the particle size of the calcite particles is less than or equal to 300 mu m to replace the induction seed crystals of the embodiment to form a new embodiment.
Different from the traditional chemical agent scale inhibition principle, the system of the invention utilizes the principle that the affinity of the same substance is far greater than that of the different substance, the induced seed crystal particles with the same or similar material as the scale crystal nucleus are added into the raw material seawater in advance, and the scale crystal nucleus crystallized and separated from the scale forming ions in the raw material seawater is preferentially deposited on the surface of the induced seed crystal. Compared with the traditional distillation desalination process, the method belongs to a physical scale inhibition method, and as long as the adsorption area provided by the added inducing seed crystal is sufficient, the separated scale crystal nucleus can be preferentially adsorbed on the surface of the inducing seed crystal, so that the higher evaporation concentration multiple can be more than 5.
In the operation process, the added induction seed crystal is preferably gypsum particles, calcite particles and the like which are the same as or similar to the seawater scale forming substances, so that the induction seed crystal has enough adsorption capacity on crystallization dirt, and the particle size of the induction seed crystal is generally not more than 300 mu m. The induced seed crystal is only needed to be added when the system is started, and the adding amount of the initial induced seed crystal is determined by calculation according to the salt content of the raw material seawater and the retention time of the feed liquid in the evaporator. After normal operation, no further addition is required.
The above-mentioned embodiments, objects, technical solutions and advantages of the present invention are further described in detail, it should be understood that the above-mentioned embodiments are only illustrative of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (2)
1. A high power concentration distillation desalination system based on an induced crystallization method, a raw material seawater feed pump (9) is connected with a condenser (4) through a pipeline, the condenser is connected with a cooling water discharge pump (12) through a cooling water pipeline, is connected with a feed valve (18) and then is connected with 3 evaporators, strong brine outlets of the 3 evaporators are respectively connected with an inlet of a forced circulation pump (10) through a strong brine pipeline, an outlet of the forced circulation pump (10) is divided into two paths, one path is connected with an outlet of the feed valve (18), and the other path is sequentially connected with inlets of a strong brine discharge valve (14) and a swirler (6); the bottom of the cyclone (6) is connected with a liquid discharge valve (15) through a pipeline and then is connected with a mother liquor tank (7), and the seed crystal tank (8) is connected with a seed crystal control valve (16), the mother liquor tank (7) and a reflux valve (17) through pipelines in sequence and then is connected with an inlet of a forced circulation pump (10); the first effect evaporator (1) is provided with a power steam inlet (20) and a first effect condensate water discharge port (21), the first effect evaporator is sequentially connected with the next stage evaporator through a secondary steam pipeline, the last effect evaporator (3) is connected with the condenser (4) through a secondary steam pipeline, the second effect evaporator, the last effect evaporator and the condenser are connected with the product water tank (5) through a product water pipeline and then connected with the product water pump (11), and the top of each effect evaporator, the upper part of the condenser (4) and the top of the product water tank (5) are respectively connected with the noncondensing control valve (19) through pipelines and then connected with the vacuum pump (13);
and a stirring device is arranged in the mother liquid tank (7).
2. A high-concentration distillation desalination method based on an induced crystallization method is characterized by comprising the following steps:
1) using a high-concentration distillation desalination system based on an induced crystallization method according to claim 1;
2) opening a raw material seawater feeding pump (9), a feeding valve (18), a forced circulation pump (10), a strong brine discharge valve (14), a liquid discharge valve (15), a cooling water discharge pump (12), a vacuum pump (13) and a noncondensable gas control valve (19), and introducing power steam into the first-effect evaporator (1) through a power steam inlet (20);
3) opening a seed crystal control valve (16), and introducing the induced seed crystal in the seed crystal tank (8) into the mother liquor tank (7);
4) raw seawater is sent into a condenser (4) through a raw seawater feeding pump (9) for preheating;
5) one part of the preheated raw material seawater is discharged by a cooling water discharge pump (12), and the other part of the preheated raw material seawater is used as a supplementary feed liquid seawater and enters 3 evaporators for evaporation after the flow rate of the supplementary feed liquid seawater is adjusted by a feed valve (18);
6) with the continuous input of power steam, the evaporation capacity of each effect evaporator is continuously increased, the water yield of the system is gradually increased, after the product water tank (5) reaches a specified liquid level, a product water pump (11) is started, the system enters a stable operation state after the water yield reaches a designed value, and a seed crystal control valve (16) is closed;
7) the power steam entering the first-effect evaporator (1) exchanges heat with the feed seawater and then is discharged from a first-effect condensate water discharge port (21), the secondary steam generated by each first-effect evaporator is introduced into the next effect for recycling, and the secondary steam generated by the last-effect evaporator is introduced into a condenser for recycling; product water generated by condensing the evaporators except the first-effect evaporator and the condenser (4) by steam enters a product water tank (5) and is discharged by a product water pump (11);
8) the residual strong brine evaporated by each effect evaporator is mixed with the reflux mother liquor from a mother liquor tank (7) controlled by a reflux valve (17), then the mixture is divided into two parts under the action of a forced circulation pump (10), one part is mixed with the seawater flowing out through a feed valve (18), the mixture enters each effect evaporator again for evaporation, and the other part is adjusted by a strong brine discharge valve (14) and then is introduced into a swirler (6);
9) after the strong brine containing the scale crystals enters the cyclone (6), coarse particles move to the bottom of the cyclone under the centrifugal separation action of the cyclone (6), crystallization mother liquor deposited at the bottom of the cyclone (6) is discharged into a mother liquor tank (7) through the flow control of a liquid discharge valve (15), and the supernatant of the cyclone is discharged as the strong brine;
10) under the action of a vacuum pump (13), the interior of each effect evaporator, the condenser (4) and the product water tank (5) are kept in a negative pressure state, and the operating temperature of each effect evaporator is adjusted within the range of 50-100 ℃;
the induction seed crystal is gypsum particles or calcite particles;
the grain diameter of the induction seed crystal is less than or equal to 300 mu m.
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| CN111777118A (en) * | 2020-06-30 | 2020-10-16 | 上海江柘环境工程技术有限公司 | Triple-effect evaporation device for treating salt-containing wastewater |
| CN112537813B (en) * | 2020-12-03 | 2022-11-04 | 莱芜市安邦冶金设备有限公司 | Evaporator for low-temperature multi-effect seawater desalination system |
| CN115450197B (en) * | 2022-08-30 | 2023-12-01 | 南京理工大学 | Method and system for reinforcing calcium sand island reef by urease catalysis based on vacuum preloading |
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