CN112408569A - Continuous treatment method of high-salinity wastewater containing sodium chloride - Google Patents
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Abstract
The invention provides a continuous treatment method of high-salinity wastewater containing sodium chloride, which comprises the steps of using a high-salinity wastewater treatment system, wherein the system comprises a freezing crystallization tower, a feeding pipe and a high-salinity wastewater feeding pump, wherein the feeding pipe and the high-salinity wastewater feeding pump are connected with the freezing crystallization tower; and a circulating cooling device used for cooling the materials in the freezing and crystallizing tower is arranged on the side of the tower, and comprises a circulating water outlet pipeline, a circulating pump, a compression refrigerator and a circulating water inlet pipeline, wherein the circulating water outlet pipeline is arranged at the middle lower part of the tower, and the circulating water inlet pipeline is arranged at the middle upper part of the tower. The method comprises the steps of continuously pumping the high-salinity wastewater into a freezing crystallization tower, collecting ice crystals at the top of the tower by a scraper device and discharging the ice crystals out of the tower; discharging the solid at the bottom of the tower into a centrifugal machine for centrifuging to obtain salt; the centrifugal mother liquor is continuously conveyed to a freezing crystallization tower through a pipeline. The ice crystal separated by the method has low content of sodium chloride and COD, the separation efficiency of the brine reaches more than 99 percent, and the wastewater after direct separation can enter biochemical treatment.
Description
Technical Field
The invention relates to the field of water treatment in the fine chemical industry, in particular to a continuous treatment method of high-salinity wastewater containing sodium chloride.
Background
In the production process of products of enterprises in the fine chemical industry, the pharmaceutical industry and the like, a large amount of high-salinity wastewater is generated, the components of the high-salinity wastewater are complex, organic matters and inorganic matters in the wastewater can not be effectively separated sometimes, and some organic matters are difficult to be completely treated by physicochemical, biochemical and other methods, so that the wastewater is difficult to achieve standard discharge. In the prior art, the traditional method for separating sodium chloride in wastewater from wastewater is evaporation concentration crystallization, such as multi-effect evaporation technology, gas-phase membrane separation and mechanical vapor recompression technology. The method has the advantages that the brine is completely separated, and the distilled fraction can directly enter the terminal biochemical treatment. However, the technology has the disadvantages that the energy consumption in the distillation process is high, and the separated sodium chloride contains a large amount of organic matters and is difficult to effectively treat.
For example, patent ZL201410796518.0 discloses a method for treating wastewater with high salt content, which comprises the following steps: high salt-containing wastewater → adjusting tank modulation → sedimentation tank chemical pretreatment → V type filter tank filtration → first stage ion exchange softening treatment → ultrafiltration system ultrafiltration → first stage reverse osmosis system reverse osmosis treatment → second stage ion exchange softening treatment → high pressure nanofiltration system nanofiltration → nanofiltration water production → second stage reverse osmosis system reverse osmosis treatment → first stage high pressure flat sheet membrane system concentration → MVR evaporative crystallization → industrial grade sodium chloride; nano-filtration concentrated water → concentration of a second section of high-pressure flat membrane system → freeze crystallization → industrial grade mirabilite; the invention reasonably couples ultrafiltration, nanofiltration, reverse osmosis and high-pressure flat membrane methods and combines the MVR crystallization and freezing crystallization technologies to treat the high-salt wastewater, overcomes the defects of a single technology, exerts the combination advantages, can treat and recover the high-salt wastewater efficiently and economically, and has remarkable economic and social benefits.
Patent ZL201510275955.2 discloses a desulfurization waste water zero release technology, including chemical medicine softening process and microfiltration membrane treatment process, and the water that comes adopts receiving and filtering and reverse osmosis separation after the two-stage softening, adopts freezing crystallization to separate out the purity of sodium sulfate decahydrate more than 99%, utilizes reverse osmosis dense water regeneration sodium ion exchange device, utilizes the evaporation crystallization to separate out the solid comprehensive utilization no liquid discharge more than 98% of sodium chloride purity. The invention can separate and reuse water in the desulfurization waste water to become usable water for life and industry, separates other impurities in the desulfurization waste water in a solid form, does not generate pollutants harmful to the natural environment, and can thoroughly solve the problem of environmental pollution caused by the desulfurization waste water.
Patent application CN201910356387.7 discloses a salt separation crystallization system for high-salinity wastewater containing organic matters, which comprises a sodium sulfate evaporation crystallization unit, a freezing crystallization unit, an organic concentration unit, a sodium chloride evaporation crystallization unit, a concentrated solution collecting tank and a miscellaneous salt drying crystallizer; also discloses a salt separation and crystallization system of the high-salinity wastewater containing organic matters, which comprises the following working procedures: evaporating and crystallizing sodium sulfate in the step (1), freezing and crystallizing in the step (2), organically concentrating in the step (3), crystallizing sodium chloride in the step (4), and drying mixed salt in the step (5). The system and the process can be used for pertinently treating the high-salinity wastewater containing the organic matters and having relatively high sulfate radical concentration, the treatment process is short, the treatment period is short, and the economic benefit of an enterprise can be ensured; in addition, the invention not only can realize the recovery of salt resources, but also can effectively ensure the purity of the recovered salt.
Patent application CN201910015558.X discloses a heat pump low temperature divides waste water treatment facilities of salt, uses the heat source heating evaporation concentration waste water of heat pump, uses the cold source freezing cooling waste water of heat pump, utilizes the characteristic that sodium sulfate solubility changes along with the temperature change, makes sodium sulfate precipitate to use the steam of secondary to carry out the evaporative crystallization of sodium chloride, the hot melt purification crystallization of sodium sulfate. The invention adopts the heat source and the cold source of the heat pump to carry out waste water desalination treatment respectively, and the energy consumption is extremely low; because of low-pressure and low-temperature evaporation, the requirement on equipment is low, a large amount of non-metallic materials can be used, and the investment is less; and has the advantages of low vibration and low noise.
In the above prior art, the methods for treating high-salinity wastewater containing sodium chloride are evaporative crystallization methods without exception. Therefore, there is a need in the art for a new method for treating high salinity wastewater containing sodium chloride.
Disclosure of Invention
The invention provides a continuous treatment method of high-salinity wastewater containing sodium chloride, which comprises the steps of using a high-salinity wastewater treatment system, wherein the high-salinity wastewater treatment system comprises a freezing crystallization tower (1), a feeding pipe and a high-salinity wastewater feeding pump (4), wherein the feeding pipe and the high-salinity wastewater feeding pump are connected with the freezing crystallization tower, and the freezing crystallization tower is an empty tower with a scraper device (11) at the top; and a circulating cooling device (2) for cooling the materials in the freezing and crystallizing tower is arranged on the side of the tower, and comprises a circulating water outlet pipeline (21) arranged at the middle lower part of the tower, a circulating pump (22), a compression refrigerator (23) and a circulating water inlet pipeline (24) arranged at the middle upper part of the tower; a solid outlet (12) is arranged at the bottom of the freezing crystallization tower, the solid outlet is communicated with a centrifugal machine (3), centrifugal mother liquor separated by the centrifugal machine is directly or indirectly injected into the freezing crystallization tower in a circulating manner, an ice crystal outlet (13) is arranged at the top or the middle upper part of the freezing crystallization tower and is used for timely sending ice crystals scraped by a scraper device (11) out of the freezing crystallization tower; the method comprises the steps of continuously pumping the high-salinity wastewater into a freezing crystallization tower, collecting ice crystals at the top of the tower by a scraper device and discharging the ice crystals out of the tower; discharging the solid at the bottom of the tower into a centrifugal machine, and centrifuging to obtain salt; the centrifugal mother liquor obtained by centrifugation is directly or indirectly continuously conveyed into a freezing crystallization tower through a pipeline.
The system can be operated continuously, and the brine separation efficiency after continuous operation can reach more than 99 percent. The waste water after the salinity separation can directly enter a biochemical treatment system for advanced treatment, so that the treatment target of the salt water separation is realized, and new three wastes are not generated in the treatment process.
In a specific embodiment, the centrifugal mother liquor separated by the centrifuge is sent back to the feeding pipe or the high-salt wastewater storage tank through a pipeline, and the centrifugal mother liquor and the high-salt wastewater are mixed before the feeding pump and are used for being circularly injected into the freezing crystallization tower.
In a specific embodiment, the feeding pipe is connected with a feeding port (14) of a freezing and crystallizing tower (1), the feeding port is positioned in the middle or middle lower part of the freezing and crystallizing tower (1), the circulating water outlet pipeline (21) is positioned below the feeding port (14), and the circulating water inlet pipeline (24) is positioned above the feeding port (14).
In a specific embodiment, the bottom of the freezing and crystallizing tower (1) is provided with a conical bottom (15) for depositing solid sodium chloride crystals.
In a specific embodiment, the sodium chloride-containing high-salt wastewater contains 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane.
In a specific embodiment, the concentration of 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane in the sodium chloride-containing high-salinity wastewater is 0.1 to 5 wt%, preferably 0.2 to 3 wt%.
In a specific embodiment, the concentration of sodium chloride in the high-salinity wastewater containing sodium chloride is 0-26.5 wt%, preferably 5-26.5 wt%.
In a specific embodiment, the rate of pumping the high-salinity wastewater from the high-salinity wastewater storage tank to the freezing and crystallizing tower (1) is more than 100kg/h, preferably 100 to 1000 kg/h.
In a specific embodiment, the feed pump and the circulation pump are both centrifugal pumps.
In a specific embodiment, the feeding pipe is arranged to exchange heat with the ice crystals in the ice crystal receiving groove (6) for collecting the ice crystals, so that the high-salinity wastewater in the feeding pipe is precooled, and meanwhile, the ice crystals in the ice crystal receiving groove (6) absorb heat to melt.
In the invention, a refrigerant pipeline in the refrigeration heat exchanger of the compression refrigerator is in full contact with a high-salinity wastewater circulating pipeline in the circulating cooling device to exchange heat.
The invention has at least the following beneficial effects: the invention uses the freezing crystallization technology, and because of no vaporization phase change process, the method has less energy consumption than the traditional evaporation concentration salt precipitation, and because of concentration under low temperature, the invention can avoid the organic matters in the high-salinity wastewater from polymerization and deterioration under high temperature, and can realize material recovery to a certain extent, thereby achieving the purpose of resource utilization. Therefore, the freezing crystallization technology has better development prospect when being applied to the treatment of wastewater containing sodium chloride. In addition, after the high-salinity wastewater is continuously treated by the freezing crystallization technology, the separated ice crystals have low sodium chloride and COD content, the separation efficiency of the brine reaches more than 99 percent, and the wastewater after direct separation can enter biochemical treatment.
Drawings
FIG. 1 shows NaCl-H2O system phase diagram.
FIG. 2 is a system diagram of a freezing crystallization treatment of high-salinity wastewater containing sodium chloride.
Detailed Description
The invention explores a novel treatment method, namely a freezing crystallization method is used for treating high-salt wastewater containing sodium chloride, and particularly the high-salt wastewater contains a certain amount of 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane. The main separation principle in the invention is as follows:
according to NaCl-H2O system phase diagram, the phase change of 25 wt% sodium chloride solution in the cooling process is shown in figure 1.
As can be seen from fig. 1, the first stage: 25 ℃ and → 2 ℃, the system is unchanged, and NaCl is saturated in the system when the temperature of the solution reaches-2 ℃. And a second stage: 2 ℃ below zero → 21.1 ℃, the solubility of NaCl is reduced along with the reduction of the system temperature, and a small amount of NaCl 2H2Separating out O, and when the temperature is reduced to-21.1 ℃, the system reaches the eutectic point temperature. And a third stage: system dimensionThe solution is maintained at a eutectic point temperature of-21.1 ℃, the concentration of the solution is 23.3 wt%, NaCl & 2H2Continuously separating out O and ice crystals according to the mass ratio of 37.6: 62.4; all the systems are made of NaCl.2H2The temperature continues to drop when both O crystals and ice crystals are present. After the NaCl aqueous solution reaches the eutectic point temperature. Soluble salt and ice crystal are separated out simultaneously, NaCl density (2.2 g/cm)3) Large, deposited at the bottom, from which the salt was centrifuged after enrichment; ice crystal density (0.9 g/cm)3) Small, the ice crystals floating on the surface of the solution are separated by a scraper, and the ice crystals are melted into water and then enter a biochemical system for treatment; thereby achieving separation of brine.
In the invention, a compression type refrigerator (compression refrigerator) is used for cooling materials in a freezing crystallization tower, and the compression type refrigerator relies on a compressor to increase the pressure of a refrigerant so as to realize a refrigeration cycle. The refrigerating machine consists of a compressor, a condenser, a refrigerating heat exchanger (evaporator), an expander or a throttling mechanism and some auxiliary equipment.
Example 1
In order to effectively evaluate the application of the freezing crystallization technology to the treatment of high-salinity wastewater containing sodium chloride in practical production, a set of pilot plant was designed, and table 1 shows a list of devices and detection devices used in a corresponding high-salinity wastewater treatment system.
TABLE 1 equipment List
The high-salinity wastewater quality and analysis method comprises the following steps: the wastewater is produced from chemical plant production wastewater, wherein the main organic matters of the wastewater are 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane and trace aniline, the COD range is 3000-4000 mg/L, the pH value is 8.0-9.0, and the sodium chloride content is about 25 wt%. The COD detection method is a dichromate method (GB11914-89), the salt content is converted according to the measured chloride ion content, the chloride ion content detection method is a silver nitrate titration method (GB/T15453-1995), the moisture detection method is a Karl Fischer method (GB6283-86), the organic matter content is obtained by calculating according to the difference value of ash and moisture, and the ash detection method refers to GB 5009.4.
The experimental process comprises the following steps: FIG. 2 is a schematic view of a high-salinity wastewater treatment system according to the present invention. The test is carried out in the system according to a batch method and a continuous freezing method in sequence, and the specific process is as follows.
Firstly, intermittently treating high-salinity wastewater:
(1) firstly, injecting 900kg of high-salinity wastewater into a freezing crystallization tower, starting a circulating pump and a compression refrigerator to perform heat exchange and refrigeration circulation, circularly cooling materials in the freezing crystallization tower, and cooling the high-salinity wastewater by a heat exchanger of the compression refrigerator;
(2) when ice crystals are separated out from the top of the freezing crystallization tower, indicating that the system reaches the eutectic point temperature, and recording the temperatures of the tower bottom and the tower top; and continuously circulating and cooling to separate out a large amount of sodium chloride crystals at the bottom of the freezing crystallization tower and ice crystals at the top. The top ice crystals are intermittently collected by a scraper into an ice crystal collecting tank, and the ice crystal generation amount in unit time is recorded. After ice crystals in the ice water collecting tank are completely melted into a water phase, detecting COD and salt content;
(3) when a large amount of solids are observed at the bottom of the freezing crystallization tower through a sight glass at the lower end of the tower, and the temperature at the bottom of the freezing crystallization tower is close to-21.5 ℃, the refrigeration cycle is stopped, the bottom solids are discharged into a centrifuge for centrifuging to remove salt, and when no solids appear in the sight glass, the discharge is stopped, namely, the discharge of the solids at the bottom of the tower into the centrifuge is stopped. Continuously starting a circulating pump, and repeating the steps for cooling and freezing crystallization circularly;
(4) and when the liquid level of the freezing and crystallizing tower is lowered to the deicing lowest position at the upper end, stopping operating the system. And discharging residual liquid in the tower, sampling, and taking the mother liquid in the centrifugal mother liquid tank and the liquid melted in the ice crystal collecting tank to respectively detect COD (chemical oxygen demand) and salt content.
Secondly, continuously freezing and crystallizing to treat high-salinity wastewater:
(1) injecting 900kg of high-salinity wastewater into a freezing crystallization tower, starting a refrigeration cycle, and circularly cooling;
(2) when ice crystals are separated out from the top of the freezing and crystallizing tower, high-salinity wastewater is continuously pumped into the freezing and crystallizing tower by a feed pump at 180 kg/h; continuously collecting ice crystals on the top of the freezing crystallization tower into an ice crystal collecting tank by a scraper, and sampling from an ice crystal outlet pipeline every 2 hours to detect COD and salt;
(3) discharging salt from the bottom of the freezing crystallization tower to a centrifuge every 2h for centrifugal desalting, wherein the salt discharging end point is based on the fact that the amount of solids in a tower bottom sight glass and a pipeline sight glass is small; mother liquor obtained by centrifugation is sent into a mother liquor tank 5, the centrifugal mother liquor in the mother liquor tank is mixed with high-salinity wastewater stock solution, and the mixture is transferred into a freezing crystallization tower by a feed pump to continue freezing crystallization treatment;
(4) the system treats 2.7t of high-salinity wastewater in total, and stops running the system after the ice crystal liquid level at the tower top is lower than the lowest position of the scraped crystal. Respectively weighing the discharged materials: materials in an ice crystal receiving tank at the top of the tower, centrifugal waste salt and residual liquid in the tower. And sampling the above samples to detect COD, salt content and the like.
The experimental results are as follows: from the intermittent operation experimental phenomenon and the recorded result, when the temperature of the bottom of the freezing and crystallizing tower reaches-21.5 ℃, a large amount of solids are separated out from the bottom of the freezing and crystallizing tower, and more ice crystals appear on the top of the tower. In this case, the crystal ice and NaCl 2H2O is simultaneously precipitated, and the temperature of minus 21.5 ℃ is the eutectic point temperature of the system. Summary the experimental test data for the batch runs are shown in table 2 below:
TABLE 2 pilot plant experimental results of batch freezing crystallization
As seen from the experimental results of table 2:
(1) the content of ice crystal salt and COD separated out from the top of the freezing crystallization tower are obviously reduced, the content of 0.23 percent of sodium chloride can not influence the activity of bacteria in a biochemical pool, and a water sample after ice crystal melting can enter a biochemical system for deep treatment to realize standard discharge.
(2) The COD of the centrifugal mother liquor after freezing and crystallizing treatment is reduced to a certain extent, and the analysis reason is probably that the solubility of organic matters in the wastewater is obviously reduced due to the reduction of the system temperature in the concentration process, and then the organic matters are accumulated in a centrifugal filter cake.
(3) The organic content in the centrifuge cake increased significantly (from about 0.32 wt% to 0.95 wt%) from the stock solution, consistent with the reasons for the COD reduction analysis of the centrifuge mother liquor as described previously.
Intermittent experiments show that after the wastewater reaches the eutectic point temperature, the ice crystal generation speed is about 100kg/h, the insoluble solid generation speed is 99kg/h, and the feed liquid temperature cannot reach the eutectic point temperature once during continuous feeding, so the high-salinity wastewater feeding flow in the continuous treatment process is set to be 180 kg/h. After a total of 10h of continuous operation, the main experimental results obtained are shown in tables 3 and 4 below:
TABLE 3 controlled sampling results in continuous freezing crystallization
TABLE 4 Pilot plant test results for continuous freeze crystallization
From the results in tables 3 and 4:
(1) the sodium chloride content in the ice crystals separated by continuous freezing crystallization is only 0.21-0.24 wt%, the COD is about 500-600 mg/L, the separated ice water meets the water inlet requirement of a biochemical system, and the treatment target of salt water separation is realized to a certain extent.
(2) The content of organic matters in the centrifugal filter cake is lower than that of the intermittent method, the organic matters are mainly products in the production process, namely 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane, and the separated NaCl & 2H2The O crystal can be applied to the production process to realize the cyclic utilization of resources.
(3) From the intermediate process sampling detection result, the ice crystal melting water sample and the centrifugal mother liquor have little fluctuation of COD and salt content, and are relatively stable as a whole, and the centrifugal mother liquor is continuously applied to the high-salt wastewater stock solution, so that the problem of concentration efficiency reduction caused by organic matter enrichment is avoided;
according to the result of 10H of continuous freezing crystallization operation, the whole system operates stably, and the waste water entering the freezing crystallization system is finally treated by ice water and NaCl & 2H2The separation is achieved in the form of O crystals,the separation efficiency of the brine is more than 99 percent (the system is operated continuously), and no new three wastes are generated in the treatment process.
In general, the invention adopts the freezing crystallization technology to treat the industrial high-salinity wastewater containing sodium chloride, and the main principle is that NaCl & 2H when the sodium chloride solution reaches the eutectic point temperature2The O crystal and the ice crystal are simultaneously separated out, and the ice and the salt are separated by utilizing the density difference between the O crystal and the ice crystal and the water, so that the aim of separating the salt and the salt from the high-salinity wastewater containing the sodium chloride is finally fulfilled. The research experiment shows that after the high-salinity wastewater is treated by the freezing crystallization technology, the content of sodium chloride in the separated ice crystals is only 0.21-0.24 wt%, the COD is about 500-600 mg/L, the separation efficiency of the brine is more than 99%, and the wastewater after direct separation can enter biochemical treatment. The content of organic matters in the separated sodium chloride is low, and the organic matters are mainly products required by production, such as 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane, and can be applied to the production process.
Compared with the traditional evaporation concentration technology, the freezing crystallization technology can realize water-salt separation by using less energy consumption, and can avoid the problems of reduced concentration efficiency, poor salt production quality and the like caused by the polymerization reaction of organic matters at high temperature. Therefore, the freezing crystallization technology can be used as a new brine separation technology in the treatment of industrial high-salinity wastewater.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions and substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (10)
1. A continuous treatment method of high-salinity wastewater containing sodium chloride comprises the steps of using a high-salinity wastewater treatment system, wherein the high-salinity wastewater treatment system comprises a freezing crystallization tower (1), a feeding pipe and a high-salinity wastewater feeding pump (4) which are connected with the freezing crystallization tower, and the freezing crystallization tower is an empty tower with a scraper device (11) at the top of the tower; and a circulating cooling device (2) for cooling the materials in the freezing and crystallizing tower is arranged on the side of the tower, and comprises a circulating water outlet pipeline (21) arranged at the middle lower part of the tower, a circulating pump (22), a compression refrigerator (23) and a circulating water inlet pipeline (24) arranged at the middle upper part of the tower; a solid outlet (12) is arranged at the bottom of the freezing crystallization tower, the solid outlet is communicated with a centrifugal machine (3), centrifugal mother liquor separated by the centrifugal machine is directly or indirectly injected into the freezing crystallization tower in a circulating manner, an ice crystal outlet (13) is arranged at the top or the middle upper part of the freezing crystallization tower and is used for timely sending ice crystals scraped by a scraper device (11) out of the freezing crystallization tower; the method comprises the steps of continuously pumping the high-salinity wastewater into a freezing crystallization tower, collecting ice crystals at the top of the tower by a scraper device and discharging the ice crystals out of the tower; discharging the solid at the bottom of the tower into a centrifugal machine, and centrifuging to obtain salt; the centrifugal mother liquor obtained by centrifugation is directly or indirectly continuously conveyed into a freezing crystallization tower through a pipeline.
2. The method as claimed in claim 1, wherein the centrifugal mother liquor separated by the centrifuge is sent back to the feeding pipe or the high-salt wastewater storage tank through a pipeline, and the centrifugal mother liquor and the high-salt wastewater are mixed before the feeding pump and then are used for circulating injection into the freezing crystallization tower.
3. The method according to claim 1, characterized in that the feed pipe is connected to a feed inlet (14) of the freezing and crystallizing tower (1), the feed inlet is located in the middle or middle-lower part of the freezing and crystallizing tower (1), the circulating water outlet pipe (21) is located below the feed inlet (14), and the circulating water inlet pipe (24) is located above the feed inlet (14).
4. The method according to claim 1, characterized in that the bottom of the freezing and crystallizing tower (1) is provided with a conical bottom (15) for depositing solid sodium chloride crystals.
5. The method of claim 1, wherein the high salinity wastewater containing sodium chloride contains 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane.
6. The method according to claim 5, wherein the concentration of 3,3 '-dimethyl-4, 4' -diaminodiphenylmethane in the sodium chloride-containing high-salinity wastewater is 0.1 to 5 wt.%, preferably 0.2 to 3 wt.%.
7. The method according to claim 1, wherein the concentration of sodium chloride in the high-salinity wastewater containing sodium chloride is 0-26.5 wt%, preferably 5-26.5 wt%.
8. The method according to claim 1, wherein the high-salinity wastewater is pumped from the high-salinity wastewater storage tank to the freezing and crystallizing tower (1) at a rate of 100kg/h or more, preferably 100 to 1000 kg/h.
9. The method of claim 1, wherein the feed pump and the circulation pump are both centrifugal pumps.
10. The method according to any one of claims 1 to 9, wherein the feeding pipe is arranged to exchange heat with the ice crystals in the ice crystal receiving groove (6) for collecting the ice crystals, so that the high-salinity wastewater in the feeding pipe is precooled, and the ice crystals in the ice crystal receiving groove (6) are melted by heat absorption.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115140750A (en) * | 2022-06-14 | 2022-10-04 | 浙江世贝恩环保工程有限公司 | Method for classifying and extracting single chloride solution from fly ash washing mixed salt wastewater |
| CN115259316A (en) * | 2022-08-05 | 2022-11-01 | 广东邦普循环科技有限公司 | Wastewater treatment method |
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