CN100448789C - Technique for treating industrial wastewater of containing sodium sulfate - Google Patents
Technique for treating industrial wastewater of containing sodium sulfate Download PDFInfo
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- CN100448789C CN100448789C CNB2006100224296A CN200610022429A CN100448789C CN 100448789 C CN100448789 C CN 100448789C CN B2006100224296 A CNB2006100224296 A CN B2006100224296A CN 200610022429 A CN200610022429 A CN 200610022429A CN 100448789 C CN100448789 C CN 100448789C
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Abstract
This invention discloses a process for treating sodium sulfate-containing industrial wastewater, which is composed of three-stage treatment systems. Each crystal separation system comprises: a crystallization kettle, a centrifugal separator, and a solution pool connected from top to bottom by pipelines. The cooling pipe of the primary crystallization kettle is connected with the cooling column of primary crystallization kettle to form a circulating pipeline of cooling. The primary solution pool is connected with the secondary crystallization kettle by pipeline. The secondary solution pool is connected with the final crystallization kettle by pipeline. The final solution pool is connected with the cooling pipe of secondary crystallization kettle by pipeline to form a circulating pipeline of cooling. The final crystallization kettle is connected with a refrigerator and an expansion water tank to form a circulating pipeline of cooling. The process has high efficiency and saved energy.
Description
Technical field
The present invention relates to vanadium product enterprise waste water treatment process, particularly handle the technology of industrial wastewater of containing sodium sulfate with the subcooling method.
Background technology
The vanadium product enterprise is in the process of producing the vanadium goods, and the waste water of generation adopts pyrosulphite sodium reduction-alkali lye neutralization, filter press and evaporation concentration process combined to handle.In the evaporation concentration treating processes, to produce a large amount of Na
2SO
4Underflow solution, in this underflow, Na
2SO
4Content reach 50%-70%.Effectively in time with the Na in this underflow
2SO
4Crystallization is separated out, and is significant to whole wastewater treatment, will bring remarkable economic efficiency and environmental benefit.Owing to imitate the Na that separator is discharged from one
2SO
4About 60 ℃-70 ℃ of underflow temperature, therefore the treatment process that adopts at present is underflow to be entered the pond, by naturally cooling to about 50 ℃ part Na
2SO
4Precipitation is separated out in crystallization, and the underflow solution on top returns 1st effective evaporator again and enters the further evaporation concentration of system, so moves in circles.Because underflow solution is not enough the cooling time in existing utility, temperature drop value was little, Na when this technology was moved
2SO
4Crystallization is not thorough, the Na that contains in the solution that retrieval system is handled again
2SO
4Concentration is higher, the Na of this concentration
2SO
4After the solution retrieval system, increased intrasystem Na
2SO
4Concentration, temperature reduces a little, Na
2SO
4Blocking pipe and transferpump after the crystallization cause system's operation very unstable, and processing efficiency is low, and the stop production to overhaul time increases.
Summary of the invention
In order to solve the problems referred to above in the present treatment process of industrial wastewater of containing sodium sulfate, the present invention proposes a kind of treatment process of industrial wastewater of containing sodium sulfate.
Described technology is made of the tertiary treatment system, be primary crystallization separation system, intermediate Crystallization Separation system, final stage Crystallization Separation system, each Crystallization Separation system includes crystallization kettle, separating centrifuge, solution pool, and crystallization kettle, separating centrifuge, solution pool communicate by the upper, middle and lower location arrangements and by the tubing system connection in each system; Cooling line in the crystallization kettle of primary crystallization separation system is connected with primary crystallization still cooling tower by exterior pipe system and communicates, and forms the refrigeration cycle pipeline; The primary solution pond directly is connected with intermediate crystallization kettle by tubing system and communicates; Secondary solution pool directly is connected with the final stage crystallization kettle by tubing system and communicates; The final stage solution pool is connected with cooling line in the intermediate crystallization kettle by tubing system and communicates, and forms the refrigeration cycle pipeline; The final stage crystallization kettle is connected with expansion tank with refrigerator by tubing system and communicates, and forms the refrigeration cycle pipeline.
Expansion tank is connected with elementary separating centrifuge, intermediate separating centrifuge, final stage separating centrifuge respectively by tubing system and communicates.
The primary solution pond directly is connected with the primary crystallization still by tubing system and communicates; Secondary solution pool directly is connected with intermediate crystallization kettle by tubing system and communicates; The final stage solution pool directly is connected with the final stage crystallization kettle by tubing system and communicates.
Cooling line in the final stage crystallization kettle is connected with first grade cooling tower cooling line by tubing system and communicates formation closed cycle piping system.
Because the present invention adopts multilevel system, and owing to be provided with many self-circulation cooling pipelines, so treatment process efficient height of the present invention, and save energy.
Description of drawings
Fig. 1 is an embodiments of the invention processing set-up synoptic diagram;
Fig. 2 is a processing set-up synoptic diagram of the present invention;
Among the figure, 1 primary crystallization still cooling tower; 2 refrigeration cycle water pumps; 3,45,46 motorized valves; 4,16,34 just,, the final stage crystallization kettle; 5Na
2SO
4Underflow solution feed pipe; 6,31,47 material wash tubes; 7,21,32 just,, the final stage separating centrifuge; 8,20,33 blowing motorized valves; 9 whizzer opening for feeds; 10 whizzer scavenging solution fluid inlets; 11,22,37 whizzer Na
2SO
4The solid discharge port; 12,23,29 separating centrifuge drain pipes; 13,39,26 just,, final stage Na
2SO
4Solution pool; 14,40,28 crystallization kettle scavenging pumps; 15,17,27 crystallization kettle wash tubes; 18,24,36 solution feed pumps; 19,35 feed flow motorized valves; 25 low temperature metabisulfite solution circulation tubes; 30 upflow tubes; 41 expansion tanks; 42 filling pipes; 43 refrigerators; 44 refrigerator cooling towers.
Embodiment
Fig. 1 shows three grades of cooling treatment systems of the present invention, be primary crystallization separation system, intermediate Crystallization Separation system, final stage Crystallization Separation system, each Crystallization Separation system includes crystallization kettle 4,16,34, separating centrifuge 7,21,32, solution pool 13,39,26, and crystallization kettle, separating centrifuge, solution pool communicate by the upper, middle and lower location arrangements and by tubing system 8,12,20,23,33,29 connections in each system; Cooling line in the crystallization kettle of primary crystallization separation system is connected with primary crystallization still cooling tower 1 by exterior pipe system 2,3 and communicates, and forms the refrigeration cycle pipeline; Primary solution pond 13 directly is connected with intermediate crystallization kettle 16 by tubing system 18,19 and communicates; Secondary solution pool 39 directly is connected with the final stage crystallization kettle by tubing system 35,36 and communicates; Final stage solution pool 26 is connected with cooling line in the intermediate crystallization kettle by tubing system 24,25 and communicates, and forms the refrigeration cycle pipeline; Final stage crystallization kettle 34 is connected with expansion tank 41 with refrigerator 43 by tubing system and communicates, and forms the refrigeration cycle pipeline.
Expansion tank is connected with elementary separating centrifuge, intermediate separating centrifuge, final stage separating centrifuge respectively by tubing system and communicates.
The primary solution pond directly is connected with the primary crystallization still by tubing system and communicates; Secondary solution pool directly is connected with intermediate crystallization kettle by tubing system and communicates; The final stage solution pool is connected with the final stage crystallization kettle by tubing system and communicates;
Cooling line in the final stage crystallization kettle is connected with first grade cooling tower cooling line by motorized valve 45,46 and communicates formation closed cycle piping system.
The Na that concentration 60-70%, temperature are about 70 ℃
2SO
4Underflow solution enters primary crystallization still 4 through feed-pipe 5. Crystallization kettle 4,16,34 internal layout have the little heat transfer tube of heat transfer efficiency height, surface adhesion force and are provided with liquid level sensor, temperature sensor, agitator etc.Liquid level sensor indication Na
2SO
4After underflow solution was filled it up with, charging stopped, and cooling tower 1 and cooling pump 2 entrys into service are cooled off the solution in the primary crystallization still 4, when temperature sensor is indicated Na in this crystallization kettle
2SO
4When underflow is cooled to 35 ℃ of left and right sides, most of Na has been arranged
2SO
4Crystal is separated out, and at this moment, cooling pump 2 and cooling tower 1 are out of service, and separating centrifuge 7 is opened automatically, reach specified speed after, the motorized valve 8 of crystallization kettle 4 bottoms is opened, the beginning fractional crystallization Na
2SO
4Solid, crystalline Na
2SO
4Solid is discharged from discharge port 11, remaining Na
2SO
4It is about about 40% that strength of solution is reduced to, and flows into solution pools 13 through the drain pipe 12 of whizzer 7, separate finish after, new Na
2SO
4Underflow solution enters primary crystallization still 4 through feed-pipe 5, like this mode refrigerated separation.
The Na of solution pool 13
2SO
4Solution is crystallization kettle 16 in the middle of solution feed pump 18, feed flow motorized valve 19 are squeezed into, liquid level sensor indication Na
2SO
4After solution is filled, open solution feed pump 24, will utilize crystallization kettle 34 by the refrigerator cooling and utilize the lower Na of concentration, temperature after whizzer 32 separates
2SO
4The cooling system of crystallization kettle 16 in the middle of solution is squeezed into, the about 35 ℃ Na that enters by solution pool 13 in the crystallization kettle in the middle of the cooling
2SO
4Solution.When this solution temperature is reduced to 20 ℃ of left and right sides, open whizzer 21, the Na of fractional crystallization
2SO
4Solid, this solid is discharged from discharge port 22, and remaining liq enters solution pool 39 through pipeline 23.
The about 20 ℃ Na of temperature in the solution pool 39
2SO
4Solution is squeezed into final stage crystallization kettle 34 by pump 36, feed flow motorized valve 35, and the water coolant that produces by refrigerator 43 crystallisation by cooling that circulates separates.
When work has just been started shooting by the entire treatment system, also be system's circulation time for the first time, crystallization kettle 34 was not also worked, and in the solution pool 26 cooling liqs was not arranged, therefore in the middle of crystallization kettle 16 the first time circulation time do not work the Na in this moment solution pool 13
2SO
4Solution directly enters solution pool 39 through water pump 18, supplying valve 19, bleeder valve 20, whizzer 21, drain pipe 23, squeezes into crystallization kettle 34 by pump 36 again.The water coolant that produces by refrigerator 43 directly cools off 35 ℃ Na
2SO
4Solution.When this solution was cooled to about 15 ℃, refrigerator 43 quit work, and bleeder valve 33 is opened, and whizzer 32 starts, the Na of beginning fractional crystallization
2SO
4, solid Na
2SO
4Discharge the Na that remaining temperature is about 15 ℃ from discharge port 37
2SO
4Solution flows into solution tank 26, this low temperature Na
2SO
4The about 35 ℃ of Na of crystallization kettle 16 temperature in the middle of solution is used for cooling off
2SO
4The water coolant of solution is circulated by water pump 24.
Na in the solution pool 26
2SO
4After solution temperature raises, send into vaporizer by upflow tube 30 and continue evaporation, enter the above-mentioned recycle system once more.
The purpose of crystallization kettle is a save energy in the middle of being provided with, the about 15 ℃ Na of temperature that promptly utilizes the final stage crystallization kettle to produce
2SO
4Solution is by the about 35 ℃ Na of temperature in the crystallization kettle in the middle of the pump 24 circulation coolings
2SO
4Solution can be with 35 ℃ Na
2SO
4Solution is cooled to about 20 ℃, can save the energy consumption of refrigerator and the energy consumption of falling-film evaporator simultaneously.
Motorized valve the 3,45, the 46th is set, brilliant in order to remove, as the water coolant and the Na of refrigerator 43 generations
2SO
4During the solution excessive temperature differentials, have some Na on the cooling tube in the crystallization kettle
2SO
4Crystal adheres to, and at this moment, after the material in the crystallization kettle 34 has been put, motorized valve 3 can cut out, and motorized valve 45,46 is opened, and makes elementary water coolant enter the heat transfer tube circulation several minutes of crystallization kettle 34, treats will to adhere to Na on the heat transfer tube automatically after temperature raises
2SO
4Crystal melts, and removes brilliant purpose automatically to reach.
The effect of pipeline 6,31,47 is that the refrigerated water washing centrifuger 7,21,32 that utilizes refrigerator to produce does not separate clean Na
2SO
4Solid.
The effect of water pump 14,24,28 and pipeline 15,17,27 is to utilize isolated separately Na
2SO
4Liquid cleans inner residual crystallisate.
This technology is finished a round-robin processing cycle and is approximately about one hour, during actual production, if crystallization kettle has one hour liquid amount, only need build underflow deposit pond again, for the on-the-spot underflow saving that flows to continuously.Investment allows also can build the same production line of two covers, is used.
This embodiment has been described a tertiary treatment technology, is designed to the tower steel structural form of three covers respectively, and cooling tower is at topmost, and middle portion is provided with crystallization kettle, and the bottom is provided with separating centrifuge, and three separating centrifuge bottoms are provided with rotary conveyor, isolated Na
2SO
4Solid can be transported or directly entrucking or pack by rotary conveyor.
This technology all adopts control automatically, water pump, cooling tower, crystallization kettle, agitator, motorized valve, separating centrifuge and refrigerator, scavenging pump are all controlled by an industrial computer, according to the treatment time requirement, weave sequence of control, carry out control automatically, and artwork, temperature parameter are presented on the computer screen, realize on-the-spot unattended.
Claims (8)
1, a kind of technique for treating industrial wastewater of containing sodium sulfate, system constitutes by tertiary treatment, be primary crystallization separation system, intermediate Crystallization Separation system, final stage Crystallization Separation system, each Crystallization Separation system includes crystallization kettle (4,16,34), separating centrifuge (7,21,32), solution pool (13,39,26), it is characterized in that crystallization kettle, separating centrifuge, solution pool communicate by the upper, middle and lower location arrangements and by the tubing system connection in each system; Cooling line in the crystallization kettle of primary crystallization separation system (4) is connected with primary crystallization still cooling tower (1) by exterior pipe system and communicates, and forms the refrigeration cycle pipeline; Primary solution pond (13) directly is connected with intermediate crystallization kettle (16) by tubing system and communicates; Secondary solution pool (39) directly is connected with final stage crystallization kettle (34) by tubing system and communicates; Final stage solution pool (26) is connected with cooling line in the intermediate crystallization kettle (16) by tubing system and communicates, and forms the refrigeration cycle pipeline; Final stage crystallization kettle (34) is connected with expansion tank (41) with refrigerator (43) by tubing system and communicates, and forms the refrigeration cycle pipeline.
2, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1, it is characterized in that expansion tank (41) is connected with elementary separating centrifuge, intermediate separating centrifuge, final stage separating centrifuge respectively by material wash tube (6,47,31) and communicates.
3, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1 and 2, it is characterized in that, cooling line in the final stage crystallization kettle (34) is connected with first grade cooling tower cooling line by motorized valve (45,46) and communicates formation closed cycle piping system.
4, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1 and 2 is characterized in that, primary solution pond (13) directly are connected with primary crystallization still (4) by tubing system and communicate.
5, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1 and 2 is characterized in that, secondary solution pool (39) directly is connected with intermediate crystallization kettle (16) by crystallization kettle wash tube (17) and communicates.
6, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1 and 2 is characterized in that, final stage solution pool (26) directly is connected with final stage crystallization kettle (34) by crystallization kettle wash tube (27) and communicates.
7, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 1 and 2 is characterized in that, primary solution pond (13) directly are connected with primary crystallization still (4) by tubing system and communicate; Secondary solution pool (39) directly is connected with intermediate crystallization kettle (16) by tubing system and communicates; Final stage solution pool (26) directly is connected with final stage crystallization kettle (34) by tubing system and communicates.
8, a kind of technique for treating industrial wastewater of containing sodium sulfate according to claim 3 is characterized in that, primary solution pond (13) directly are connected with primary crystallization still (4) by tubing system and communicate; Secondary solution pool (39) directly is connected with intermediate crystallization kettle (16) by tubing system and communicates; Final stage solution pool (26) directly is connected with final stage crystallization kettle (34) by tubing system and communicates.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100224296A CN100448789C (en) | 2006-12-05 | 2006-12-05 | Technique for treating industrial wastewater of containing sodium sulfate |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100224296A CN100448789C (en) | 2006-12-05 | 2006-12-05 | Technique for treating industrial wastewater of containing sodium sulfate |
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| CN101003411A CN101003411A (en) | 2007-07-25 |
| CN100448789C true CN100448789C (en) | 2009-01-07 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103880209A (en) * | 2014-03-12 | 2014-06-25 | 广东宇星阻燃新材有限公司 | Processing method of sodium sulfate wastewater |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102616891B (en) * | 2011-12-31 | 2014-07-09 | 广东先导稀材股份有限公司 | Method for treating sewage containing sodium sulfate and sodium chloride |
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| EP0427401A1 (en) * | 1989-10-11 | 1991-05-15 | W.R. Grace & Co.-Conn. | Conversion of iminodiacetic acid crystal liquors to concentrated solutions of monoalkalimetal or monoammonium iminodiacetate |
| CN1045432C (en) * | 1997-05-22 | 1999-10-06 | 南开大学新技术集团公司丹阳分厂 | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid |
| CN1462741A (en) * | 2003-06-23 | 2003-12-24 | 余姚市东泰精细化工有限公司 | Method for preparing sodium methallyl sulfonic acid |
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2006
- 2006-12-05 CN CNB2006100224296A patent/CN100448789C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0427401A1 (en) * | 1989-10-11 | 1991-05-15 | W.R. Grace & Co.-Conn. | Conversion of iminodiacetic acid crystal liquors to concentrated solutions of monoalkalimetal or monoammonium iminodiacetate |
| CN1045432C (en) * | 1997-05-22 | 1999-10-06 | 南开大学新技术集团公司丹阳分厂 | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid |
| CN1462741A (en) * | 2003-06-23 | 2003-12-24 | 余姚市东泰精细化工有限公司 | Method for preparing sodium methallyl sulfonic acid |
Non-Patent Citations (4)
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| 五氧化二钒生产中钠盐的排放与回收利用. 高航.铁合金，第3期. 2000 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103880209A (en) * | 2014-03-12 | 2014-06-25 | 广东宇星阻燃新材有限公司 | Processing method of sodium sulfate wastewater |
| CN103880209B (en) * | 2014-03-12 | 2015-08-12 | 广东宇星阻燃新材有限公司 | A kind for the treatment of process of sodium sulfate wastewater |
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| CN101003411A (en) | 2007-07-25 |
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