CN210825804U - Special equipment for evaporative crystallization process for reducing salt impurity rate - Google Patents
Special equipment for evaporative crystallization process for reducing salt impurity rate Download PDFInfo
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- CN210825804U CN210825804U CN201920913688.0U CN201920913688U CN210825804U CN 210825804 U CN210825804 U CN 210825804U CN 201920913688 U CN201920913688 U CN 201920913688U CN 210825804 U CN210825804 U CN 210825804U
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Abstract
The utility model discloses a reduce professional equipment of evaporative crystallization technology of miscellaneous salt rate obtains industrial salt one through evaporation crystallization, centrifugal drying for the first time with evaporation inflow, and centrifugal drying's mother liquor for the first time gets into evaporation crystallization, centrifugal drying for the second time and obtains industrial salt two, and industrial salt two-way dissolves to return evaporation inflow through the retrieval and utilization water. The utility model discloses a combination of secondary evaporation crystal system, effective lowering system produces miscellaneous salt volume, improves the purity of evaporation crystal system industrial salt, realizes resource utilization to the zero release of waste water has been realized.
Description
Technical Field
The utility model belongs to the technical field of industrial wastewater treatment, in particular to a special device for an evaporative crystallization process for reducing the salt impurity rate.
Background
A large amount of high-salt high-organic wastewater is generated in the industrial production processes of petrochemical industry, coal chemical industry, metallurgy, pharmacy, printing and dyeing, papermaking and the like, the salt content is usually more than 3000mg/L, the COD concentration is more than 2000mg/L, and the wastewater contains a large amount of toxic and harmful organic matters such as aromatic compounds, heterocyclic compounds, hydrocarbon compounds and the like. Zero discharge of wastewater is the final target required to be realized in the industrial wastewater industry at present and is an important link for realizing sustainable and stable development. In the development process of the zero emission technology, industrial salt produced by evaporative crystallization contains some organic substances, so that the quality of the industrial salt is poor, resource utilization cannot be realized, and the industrial salt can only be treated as hazardous waste generally, which is a bottleneck for limiting the realization of zero emission.
The treatment method for strong brine at home and abroad at present generally comprises the following steps: efficient oxidation, reverse osmosis, forward osmosis, electric desalination, membrane distillation, and the like. Despite many methods, organic matters still remain in the crystallized salt obtained by evaporation and crystallization, and finally industrial salt with high quality cannot be obtained, so that the disposal cost is high, the environment is harmed if the industrial salt is not disposed, and simultaneously, the resource waste is also caused. Therefore, how to improve the evaporative crystallization technology and realize high-quality reuse of industrial salt is not only a development trend of various industries but also an inevitable requirement for environmental protection.
Regarding the evaporative crystallization process for reducing the salt impurity rate, chinese patent CN201510054597.2 discloses a method for recovering and treating high-salt wastewater, which recovers sodium sulfate and sodium chloride through three treatment steps of primary evaporative crystallization, cooling crystallization and secondary evaporative crystallization. The process is simple and stable, can effectively recover sodium sulfate and sodium chloride in the wastewater, and increases energy consumption and investment cost by using a twice evaporation and once cooling crystallization mode.
Regarding the evaporative crystallization process for reducing the salt impurity rate, chinese patent CN201610618267.6 discloses a treatment method of high-salinity wastewater, which recovers sodium sulfate and sodium chloride through five treatment steps of one-effect heating, one-time evaporative crystallization, cooling crystallization, two-effect heating and secondary evaporative crystallization. The process shortens the treatment time and reduces the environmental protection pressure through one-effect heating and two-effect heating. Similar to the above patents, the treatment of high concentration brine also has the problems of high energy consumption and high investment cost.
SUMMERY OF THE UTILITY MODEL
The utility model discloses to the engineering difficult problem that the miscellaneous salt production volume of evaporation crystallization is big, investment running cost is high among the strong brine processing procedure, provide a professional equipment that reduces the evaporation crystallization technology of miscellaneous salt rate, its characterized in that: the system comprises a first forced circulation evaporator, a first forced circulation evaporation heater, a first thickener, a first centrifuge, a first salt collecting system, a first mother liquor tank, a first steam compressor, a first condensed water tank, a first heat exchanger, a second forced circulation evaporator, a second forced circulation evaporation heater, a second thickener, a second centrifuge, a second salt collecting system, a second mother liquor tank, a second steam compressor, a second condensed water tank and a second heat exchanger;
the raw water tank is connected with the feed end of the first heat exchanger, a feed pump is arranged on the connecting pipeline, the discharge port of the first heat exchanger is connected with the feed port of the first forced circulation pump through a first forced circulation pipe, the discharge port of the first forced circulation pump is connected with the feed port of the first forced circulation evaporator through a first forced circulation evaporation heater, the condensed water outlet of the first forced circulation evaporation heater is connected with the inlet of a first condensed water tank, the water outlet of the first condensed water tank is connected with the water inlet of the first heat exchanger through a first condensed water pump, the water outlet of the first heat exchanger is connected with a reuse water tank, the bottom of the first forced circulation evaporator is connected with a first thickener, and the outlet of the first thickener is connected with the inlet of a first centrifuge; a crystallized salt outlet of the primary centrifuge is connected with a primary salt collecting system; a mother liquor outlet of the primary centrifuge is connected with a feed inlet of a primary mother liquor tank; the discharge port of the first mother liquor tank is respectively connected with the feed port of the second heat exchanger and the first forced circulation pipe, a second mother liquor pump and a first mother liquor pump are respectively and correspondingly arranged on the connecting pipeline, and the discharge port of the second heat exchanger is connected with the feed port of the second forced circulation pump through the second forced circulation pipe; a discharge hole of the second forced circulation pump is connected with a feed hole of the second forced circulation evaporator through a second forced circulation evaporation heater, a condensed water outlet of the second forced circulation evaporation heater is connected with an inlet of a second condensed water tank, and a water outlet of the second condensed water tank is connected with a water inlet of the second heat exchanger through a second condensed water pump; the water outlet of the secondary heat exchanger is connected with a reuse water pool; the bottom of the second forced circulation evaporator is connected with the second thickener; the outlet of the secondary thickener is connected with the inlet of the secondary centrifuge; a crystallized salt outlet of the secondary centrifuge is connected with a secondary salt collecting system; a mother liquor outlet of the secondary centrifuge is connected with a feed inlet of a secondary mother liquor tank; the discharge hole of the second mother liquor tank is connected to a second forced circulation pipe through a second mother liquor reflux pump.
Further, the first forced circulation evaporator and the second forced circulation evaporator are multi-effect evaporators or MVR evaporators, and the bottom parts of the first forced circulation evaporator and the second forced circulation evaporator are respectively provided with an elutriation leg for preventing salt from accumulating at the bottom part to block an outlet;
the steam outlet of the first forced circulation evaporator is connected with the steam inlet of the first forced circulation evaporation heater through a first steam compressor, and an auxiliary steam inlet is arranged on the connecting pipeline;
the steam outlet of the second forced circulation evaporator is connected with the steam inlet of the second forced circulation evaporation heater through a second steam compressor, and an auxiliary steam inlet is arranged on the connecting pipeline;
and the first forced circulation pump and the second forced circulation pump adopt forced circulation pumps.
Advantageous effects
The utility model provides a pair of reduce professional equipment of evaporation crystallization technology of miscellaneous salt rate intakes through twice evaporation crystallization technology of modified and handles, and furthest reduces miscellaneous salt production volume, realizes the most genuine zero release of coal industry strong brine evaporation crystallization technology section. Wherein the discharge amount of the primary mother liquor is small, and the processing scale of the secondary evaporative crystallization system is small, so that the investment operation cost and the hazardous waste disposal cost are reduced.
Drawings
Fig. 1 is a process flow diagram of an embodiment of the present invention.
Fig. 2 is a schematic diagram of the connection relationship of the dedicated device in the embodiment of the present invention.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and examples.
Examples
As shown in the attached figure 2, the special equipment for the evaporative crystallization process for reducing the impurity salt rate comprises a first forced circulation evaporator 1, a first forced circulation evaporation heater 2, a first thickener 3, a first centrifuge 4, a first salt collection system 5, a first mother liquor tank 6, a first steam compressor 7, a first condensed water tank 8, a first heat exchanger 9, a second forced circulation evaporator 10, a second forced circulation evaporation heater 11, a second thickener 12, a second centrifuge 13, a second salt collection system 14, a second mother liquor tank 15, a second steam compressor 16, a second condensed water tank 17 and a second heat exchanger 18;
the raw water tank 19 is connected with the feed end of the first heat exchanger 9, the connecting pipeline is provided with a feed pump 20, the discharge hole of the first heat exchanger 9 is connected with the feed inlet of a first forced circulation pump 21 through a first forced circulation pipe 28, the discharge hole of the first forced circulation pump 21 is connected with the feed inlet of a first forced circulation evaporator 1 through a first forced circulation evaporation heater 2, the condensed water outlet of the first forced circulation evaporation heater 2 is connected with the inlet of a first condensed water tank 8, the water outlet of the first condensed water tank 8 is connected with the water inlet of the first heat exchanger 9 through a first condensed water pump 22, the water outlet of the first heat exchanger 9 is connected with a reuse water pool, the bottom of the first forced circulation evaporator 1 is connected with a first thickener 3, and the outlet of the first thickener 3 is connected with the inlet of a first centrifuge 4; a crystallized salt outlet of the primary centrifuge 4 is connected with a primary salt collecting system 5; a mother liquor outlet of the first centrifuge 4 is connected with a feed inlet of a first mother liquor tank 6; the discharge hole of the first mother liquor tank 6 is respectively connected with the feed hole of the second secondary heat exchanger 18 and a first forced circulation pipe 28, a second mother liquor pump 23 and a first mother liquor pump 24 are respectively and correspondingly arranged on the connecting pipelines, and the discharge hole of the second secondary heat exchanger 18 is connected with the feed hole of a second forced circulation pump 25 through a second forced circulation pipe 29; a discharge port of the second forced circulation pump 25 is connected with a feed port of the second forced circulation evaporator 10 through the second forced circulation evaporation heater 11, a condensed water outlet of the second forced circulation evaporation heater 11 is connected with an inlet of the second condensed water tank 17, and a water outlet of the second condensed water tank 17 is connected with a water inlet of the second heat exchanger 18 through a second condensed water pump 26; the water outlet of the secondary heat exchanger 18 is connected with a reuse water pool; the bottom of the second forced circulation evaporator 10 is connected with a second thickener 12; the outlet of the second thickener 12 is connected with the inlet of the second centrifuge 13; a crystallized salt outlet of the secondary centrifuge 13 is connected with a secondary salt collecting system 14; a mother liquor outlet of the secondary centrifuge 13 is connected with a feed inlet of a secondary mother liquor tank 15; the discharge port of the second-time mother liquor tank 15 is connected to a second-time forced circulation pipe 29 through a second mother liquor reflux pump 27.
The first forced circulation evaporator 1 and the second forced circulation evaporator 10 are multi-effect evaporators or MVR evaporators, and the bottom parts of the first forced circulation evaporator and the second forced circulation evaporator are respectively provided with an elutriation leg for preventing salt from accumulating at the bottom part to block an outlet;
a steam outlet of the first forced circulation evaporator 1 is connected with a steam inlet of the first forced circulation evaporation heater 2 through a first steam compressor 7, and an auxiliary steam inlet is arranged on a connecting pipeline;
the steam outlet of the second forced circulation evaporator 10 is connected with the steam inlet of the second forced circulation evaporation heater 11 through a second secondary steam compressor 16, and an auxiliary steam inlet is arranged on the connecting pipeline;
the first forced circulation pump 21 and the second forced circulation pump 25 are forced circulation pumps.
As shown in the attached figure 1, the evaporative crystallization process for reducing the salt impurity rate by using the special equipment comprises the following steps:
firstly, evaporating inlet water to obtain first product water through a first evaporation crystallization process, wherein the first product water is produced after high-concentration brine is subjected to pretreatment, impurity precipitation, softening, oxidation, membrane separation and other processes. Wherein the temperature of the materials is controlled between 65 ℃ and 110 ℃, the pH is between 8 and 9, the vacuum degree is between 0.025 MPa and 0.150MPa, and the water produced by the first evaporation crystallization enters the next step.
The second step, the first produced water obtained in the first step is subjected to first centrifugal drying to obtain a first mother liquor and a first industrial salt, the rotating speed of the centrifugal machine is 1500-2200r/min, the temperature is controlled at 60-80 ℃, the obtained first industrial salt enters a first salt collecting system, the obtained first mother liquor enters the next step, wherein the total TDS of water soluble solids of the first mother liquor is 300000-400000mg/L, and Cl is-The concentration reaches 130000-180000mg/L or SO4 2-The concentration is 20000-30000 mg/L.
And thirdly, carrying out secondary evaporation crystallization on the mother liquor I in the second step to obtain second produced water, controlling the temperature to be 80-100 ℃, controlling the pH value to be 8-9 and the vacuum degree to be 0.048-0.10MPa, and entering the next step when the second produced water is obtained.
And fourthly, carrying out secondary centrifugal drying on the second water product in the third step to obtain a second mother solution and a second industrial salt, returning the second mother solution to the second evaporation and crystallization, controlling the rotating speed of the centrifugal machine at 1500-2200r/min and the temperature at 60-80 ℃, and carrying out a secondary salt collection system on the obtained second industrial salt.
And fifthly, dissolving the industrial salt II in the fourth step by using the reuse water, returning the industrial salt II to the evaporation water inlet, and dissolving by using the condensed water obtained by twice evaporation crystallization.
Wherein, in the second step, when the total TDS of the soluble solids of the mother liquor I is within 300000mg/L, Cl-The concentration is within 130000mg/L or SO4 2-The concentration is within 20000mg/L, and the mother liquor is returned to the first step for further processingThe first evaporation crystallization is carried out, and the temperature is controlled to be 60-80 ℃.
The utility model provides a pair of reduce professional equipment of evaporation crystallization technology of miscellaneous salt rate intakes through twice evaporation crystallization technology of modified and handles, and furthest reduces miscellaneous salt production volume, realizes the most genuine zero release of coal industry strong brine evaporation crystallization technology section. Wherein the discharge amount of the primary mother liquor is small, and the processing scale of the secondary evaporative crystallization system is small, so that the investment operation cost and the hazardous waste disposal cost are reduced.
Claims (2)
1. A special device for reducing the miscellaneous salt rate of an evaporative crystallization process is characterized in that: the system comprises a first forced circulation evaporator (1), a first forced circulation evaporation heater (2), a first thickener (3), a first centrifuge (4), a first salt collection system (5), a first mother liquor tank (6), a first steam compressor (7), a first condensed water tank (8), a first heat exchanger (9), a second forced circulation evaporator (10), a second forced circulation evaporation heater (11), a second thickener (12), a second centrifuge (13), a second salt collection system (14), a second mother liquor tank (15), a second steam compressor (16), a second condensed water tank (17) and a second heat exchanger (18);
the raw water tank (19) is connected with the feed end of the first heat exchanger (9), a feed pump (20) is arranged on the connecting pipeline, the discharge port of the first heat exchanger (9) is connected with the feed port of the first forced circulation pump (21) through a first forced circulation pipe (28), the discharge port of the first forced circulation pump (21) is connected with the feed port of the first forced circulation evaporator (1) through a first forced circulation evaporation heater (2), the condensed water outlet of the first forced circulation evaporation heater (2) is connected with the inlet of the first condensed water tank (8), the water outlet of the first condensed water tank (8) is connected with the water inlet of the first heat exchanger (9) through a first condensed water pump (22), the water outlet of the first heat exchanger (9) is connected with a reuse water pool, the bottom of the first forced circulation evaporator (1) is connected with the first thickener (3), the outlet of the first thickener (3) is connected with the inlet of the first centrifuge (4); a crystallized salt outlet of the primary centrifuge (4) is connected with a primary salt collecting system (5); a mother liquor outlet of the primary centrifuge (4) is connected with a feed inlet of a primary mother liquor tank (6); the discharge hole of the first primary mother liquor tank (6) is respectively connected with the feed inlet of the second secondary heat exchanger (18) and the first forced circulation pipe (28), a second primary mother liquor pump (23) and a first primary mother liquor pump (24) are respectively and correspondingly arranged on the connecting pipeline, and the discharge hole of the second secondary heat exchanger (18) is connected with the feed inlet of the second forced circulation pump (25) through a second forced circulation pipe (29); a discharge hole of the second forced circulation pump (25) is connected with a feed hole of the second forced circulation evaporator (10) through a second forced circulation evaporation heater (11), a condensed water outlet of the second forced circulation evaporation heater (11) is connected with an inlet of a second condensed water tank (17), and a water outlet of the second condensed water tank (17) is connected with a water inlet of a second heat exchanger (18) through a second condensed water pump (26); the water outlet of the secondary heat exchanger (18) is connected with a reuse water pool; the bottom of the second forced circulation evaporator (10) is connected with a second thickener (12); the outlet of the second thickener (12) is connected with the inlet of the second centrifuge (13); a crystallized salt outlet of the secondary centrifuge (13) is connected with a secondary salt collecting system (14); a mother liquor outlet of the secondary centrifuge (13) is connected with a feed inlet of a secondary mother liquor tank (15); the discharge port of the second mother liquor tank (15) is connected to a second forced circulation pipe (29) through a second mother liquor reflux pump (27).
2. The special equipment for the evaporative crystallization process for reducing the rate of miscellaneous salts as claimed in claim 1, wherein: the first forced circulation evaporator (1) and the second forced circulation evaporator (10) are multi-effect evaporators or MVR evaporators, and the bottom parts of the first forced circulation evaporator and the second forced circulation evaporator are respectively provided with an elutriation leg for preventing salt from accumulating at the bottom part to block an outlet;
a steam outlet of the first forced circulation evaporator (1) is connected with a steam inlet of the first forced circulation evaporation heater (2) through a first steam compressor (7), and an auxiliary steam inlet is arranged on a connecting pipeline;
a steam outlet of the second forced circulation evaporator (10) is connected with a steam inlet of the second forced circulation evaporation heater (11) through a second secondary steam compressor (16), and an auxiliary steam inlet is arranged on a connecting pipeline;
the first forced circulation pump (21) and the second forced circulation pump (25) adopt forced circulation pumps.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110183022A (en) * | 2019-06-18 | 2019-08-30 | 上海晶宇环境工程股份有限公司 | A kind of evaporative crystallization technique and special equipment reducing carnallite rate |
| CN114044600A (en) * | 2021-11-23 | 2022-02-15 | 青岛康景辉环境科技集团有限公司 | High-salt high-COD wastewater treatment equipment and process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110183022A (en) * | 2019-06-18 | 2019-08-30 | 上海晶宇环境工程股份有限公司 | A kind of evaporative crystallization technique and special equipment reducing carnallite rate |
| CN114044600A (en) * | 2021-11-23 | 2022-02-15 | 青岛康景辉环境科技集团有限公司 | High-salt high-COD wastewater treatment equipment and process |
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