CN204079685U - A kind for the treatment of unit of high salinity high-COD waste water - Google Patents
A kind for the treatment of unit of high salinity high-COD waste water Download PDFInfo
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- CN204079685U CN204079685U CN201420413880.0U CN201420413880U CN204079685U CN 204079685 U CN204079685 U CN 204079685U CN 201420413880 U CN201420413880 U CN 201420413880U CN 204079685 U CN204079685 U CN 204079685U
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Abstract
The utility model discloses a kind for the treatment of unit of high salinity high-COD waste water, comprise wastewater feed pump, distillation tower, sulfate crystal still and toluene extraction tower, wastewater feed pump is connected with distillation tower, distillation tower top gas phase discharge port connects condenser, condenser is connected with vacuum system, discharge gate bottom distillation tower, be connected with sulfate crystal still, discharge port bottom sulfate crystal still is connected with separating centrifuge, separating centrifuge is connected with filtrate surge tank, filtrate surge tank is connected with filtrate dnockout pump, filtrate dnockout pump outlet is connected with toluene extraction tower, extraction wastewater discharge port bottom toluene extraction tower is connected with Sewage treatment systems.Wastewater treatment equipment of the present utility model, can reduce the salinity in the waste water in production process and COD greatly, and recycling the sodium sulfate crystal that obtains can also carry out second stage employ, further like this reduces cost, has saved resource.
Description
Technical field
The utility model relates in a kind of dicumyl peroxide production process the treatment unit of the high salinity high-COD waste water produced, and belongs to chemical plant installations field.
Background technology
At present, industrial production dicumyl peroxide is mainly raw material with isopropyl benzene, and oxidation obtains hydrogen phosphide cumene, carry out reduction reaction with sodium sulphite, generate α, alpha-alpha-dimethyl benzylalcohol, then, under perchloric acid catalysis, hydrogen phosphide cumene and benzylalcohol carry out condensation reaction and obtain product.In reduction reaction process, sodium sulphite enters into reaction system in form of an aqueous solutions.After reaction terminates, profit is separated mutually automatically, and mother-liquor waste water contains a large amount of sodium sulfate byproduct and unreacted sodium sulphite.Wherein sodium sulfate is about 25-35%, sodium sulphite is about 0.01-0.05%, and also containing isopropyl benzene, hydrogen phosphide cumene, α, the organism refuses such as alpha-alpha-dimethyl benzylalcohol, alpha-methyl styrene, methyl phenyl ketone, make COD up to 15000-20000mg/L.
High density inorganic salt in waste water can produce very strong inhibition to the microorganism active of subsequent biochemical process.Current, this waste water mainly by after large water gaging dilution, makes salinity lower than the malicious thresholding of biochemistry.But a large amount of dilution waters adds the scale of subsequent disposal, add running cost expense, serious waste water resources.And in waste water, a large amount of sodium sulfate salts cannot be recycled, and also there is waste problem to favourable resource.Simultaneously in waste water, a large amount of organism refuses also can affect the biodegradability of waste water, and COD is too high, and also severe contamination environment, is harmful to human body and biological health.
Therefore, be necessary to develop a kind of device that effectively can process high salinity high-COD waste water.
Summary of the invention
Goal of the invention: in order to solve the problems of the prior art, the utility model provides a kind for the treatment of unit of high salinity high-COD waste water.
Technical scheme: to achieve these goals, the utility model have employed following technical scheme:
A kind for the treatment of unit of high salinity high-COD waste water, comprise wastewater feed pump, distillation tower, sulfate crystal still and toluene extraction tower, described wastewater feed pump outlet is provided with wastewater feed pipeline, and be connected with described distillation tower by described wastewater feed pipeline, described distillation tower top is provided with gas phase discharge port, described gas phase discharge port is connected with overhead gas discharge pipe, described overhead gas discharge pipe is connected with condenser, the gaseous phase outlet of described condenser is connected with non-cold air discharge pipe, described non-cold air discharge pipe is connected with vacuum system, condensate outlet is provided with bottom described condenser, described condensate outlet is connected with phlegma discharge pipe, described phlegma discharge pipe is connected with distillation wastewater collection tank, discharge gate is provided with bottom described distillation tower, described discharge gate is connected with described sulfate crystal still by pipeline, discharge port bottom described sulfate crystal still is connected with crystallization kettle discharge pipe, described crystallization kettle discharge pipe is connected with separating centrifuge, described separating centrifuge is connected with centrifugation filtrate discharge pipe, described centrifugation filtrate discharge pipe is connected with filtrate surge tank, discharge port bottom described filtrate surge tank is connected with filtrate dnockout pipeline, described filtrate dnockout pipeline is connected with filtrate dnockout pump, described filtrate dnockout pump outlet is connected with feed solution pipeline, described feed solution pipeline is connected with described toluene extraction tower, extraction wastewater discharge port is provided with bottom described toluene extraction tower, described extraction wastewater discharge port is connected with sink drainage.Wastewater treatment equipment of the present utility model, first distillation tower is adopted to carry out underpressure distillation to waste water, tentatively can reduce the salinity in waste water and COD content like this, then the low salt after distillation, the distillation waste water of low COD is directly by collecting after overhead condenser cooling, and remaining high density salinity, the vinasse of high COD enters into sulfate crystal still, the sodium sulfate in crystallisation process recovery distillation residue is carried out by sulfate crystal still, and the crystallization filtrate of remaining sodium sulfate enters into toluene extraction tower again, by the organic substance in toluene extraction filtrate, reduce the COD in waste water, aqueous phase after extraction, its salinity and COD are very low, then just the salinity after process and the waste water of low COD can be drained into Sewage treatment systems to be further processed.Like this by progressive process, the salinity in the waste water in production process and COD can be reduced greatly, and without the need to being carried out dilution process by a large amount of water, save water resources, reduce scale and the cost of process waste water, and recycling the sodium sulfate crystal obtained can also carry out second stage employ, further like this reduce cost, save resource.
Be provided with column plate in described distillation tower tower, be provided with reboiler outside tower, described reboiler is provided with steam inlet and water of condensation discharge port.Heated by reboiler, make distillation tower carry out distillation waste water, heating is more even, and distilling effect is better, is provided with column plate, can improves the contact area of gas-liquid two-phase during distillation, improves distilling effect.
Described vacuum system comprises vacuum buffer tank and vacuum pump, described vacuum buffer tank is connected with the gaseous phase outlet of described condenser by described non-cold air discharge pipe, described vacuum buffer tank top is provided with gaseous phase outlet, described gaseous phase outlet is connected with vacuum pipe, described vacuum pipe is connected with described vacuum pump, described vacuum buffer pot bottom is provided with phlegma discharge port, described phlegma discharge port is connected with vacuum buffer tank phlegma discharge pipe, described vacuum buffer tank phlegma discharge pipe and described phlegma discharge pipe merge and are connected to described distillation wastewater collection tank.Vacuum buffer tank plays the effect of buffering, avoids not cooling steam completely and directly enters into vacuum pump, damages vacuum pump, serves the effect of protection vacuum pump.
The end socket of described condenser is provided with refrigerated water import and the outlet of refrigerated water backwater.The effect of refrigerated water cooling down is much higher than the cooling performance of common water of condensation.
Bottom described distillation tower, discharge gate is connected with distillation residue discharge pipe, described distillation residue discharge pipe is connected with distillation residue dnockout pump, described distillation residue dnockout pump outlet is connected with crystallization kettle feed pipe, and described crystallization kettle feed pipe is connected with described sulfate crystal still top.After distillation residue discharge pipe makes distillation, remaining high salinity height COD waste liquid enters into sulfate crystal still and processes further, distillation residue dnockout pump makes solid-liquid two in distillation debris mix, be beneficial to next step crystallization treatment on the one hand, on the other hand, in order to avoid the sodium sulfate of the inside precipitates cause line clogging.
Described sulfate crystal still inside is provided with mechanical stirring, and at the bottom of the still of described sulfate crystal still and still top is respectively equipped with refrigerated water import and the outlet of refrigerated water backwater, adopts the cooling of refrigerated water inner coil pipe.Internal cooling is relative to exterior cooling, and cooling performance is better, refrigerated water, and temperature is lower than common condensate temperature, cooling performance is better, adds mechanical stirring, waste liquid is mixed, during crystallization treatment, the impurity wrapped up in the crystal obtained is less, and the crystal purity of recovery is higher.
Described separating centrifuge inside is provided with water wash system, described water wash system is connected with washing water pipeline, the distillation phlegma that described washing water pipeline obtains by carrying out through described distillation tower and condenser distilling, after condensation causes described separating centrifuge, and described separating centrifuge is provided with sodium sulfate drainage line.Water wash system is washed reclaiming the sodium sulfate crystal obtained in crystallization kettle, improves the purity of the crystal reclaimed; The distillation phlegma that washing water pipeline obtains by carrying out through described distillation tower and condenser distilling, after condensation causes described separating centrifuge and fully recycles water resources, save energy.
Described toluene extraction tower middle and upper part is provided with wastewater feed mouth, is provided with toluene feed mouth in middle and lower part.Extracting toluene discharge port is provided with at top.
Principle of work: principle of work of the present utility model is as follows:
The mother-liquor waste water produced in production process by vacuum still, by oily water separation.The distillation waste water of low salt, low COD is by collecting after overhead condenser cooling.Vinasse containing high density salinity, high COD enters sulfate crystal still crystallisation by cooling.Sodium sulfate crystal removes mother liquor through centrifugation, then removes impurity further with the water of condensation washing of low temperature, obtains the sodium sulfate crystal that purity is high.Isolated filtrate salinity is low, but COD content is high.Extracted by toluene, will significantly reduce the COD of filtrate.Filtrate after extraction directly enters Sewage treatment systems.Toluene after extraction uses by Distillation recovery.
Beneficial effect: adopt the utility model of technique scheme to have following advantage:
Specifically, compared with prior art, the technical solution of the utility model has following outstanding advantage:
1, wastewater treatment equipment of the present utility model, first distillation tower is adopted to carry out underpressure distillation to waste water, tentatively can reduce the salinity in waste water and COD content like this, then the low salt after distillation, the distillation waste water of low COD is directly by collecting after overhead condenser cooling, and remaining high density salinity, the vinasse of high COD enters into sulfate crystal still, the sodium sulfate in crystallisation process recovery distillation residue is carried out by sulfate crystal still, and the crystallization filtrate of remaining sodium sulfate enters into toluene extraction tower again, by the organic substance in toluene extraction filtrate, reduce the COD in waste water, aqueous phase after extraction, its salinity and COD are very low, then just the salinity after process and the waste water of low COD can be drained into Sewage treatment systems to be further processed.Like this by progressive process, the salinity in the waste water in production process and COD can be reduced greatly, and without the need to being carried out dilution process by a large amount of water, save water resources, reduce scale and the cost of process waste water, and recycling the sodium sulfate crystal obtained can also carry out second stage employ, further like this reduce cost, save resource;
2, the utility model is provided with distillation residue dnockout pump, filtrate dnockout pump, pending mixture solid-liquid is mixed, is more beneficial to next step process;
3, cooling system of the present utility model, adopt refrigerated water, cooling performance is better;
4, the water wash system of separating centrifuge of the present utility model, the distillation phlegma fully recycled that distillation tower and condenser carry out distilling, obtain after condensation, recycles distillation phlegma as washing water, has saved the energy;
5, the utility model has the processing efficiency of stability and high efficiency, and distillation waste water and sodium sulfate all can reclaim use, saved resource, avoided secondary pollution.
Accompanying drawing explanation
Fig. 1 is the connection schematic flow sheet of the utility model embodiment;
In figure: 1-distillation tower, 2-reboiler, 3-condenser, 4-vacuum buffer tank, 5-distills wastewater collection tank, 6-sulfate crystal still, 7-separating centrifuge, 8-filtrate surge tank, 9-extraction tower, 10-wastewater feed pump, 11-vacuum pump, 12-distillation residue dnockout pump, 13-filtrate dnockout pump, 14-wastewater feed pipeline, 15-overhead gas discharge pipe, the non-cold air discharge pipe of 16-, 17-vacuum pipe, 18-vacuum buffer tank phlegma discharge pipe, 19-phlegma discharge pipe, 20-washing water pipeline, 21-distillation residue discharge pipe, 22-crystallization kettle feed pipe, 23-crystallization kettle discharge pipe, 24-sodium sulfate drainage line, 25-centrifugation filtrate discharge pipe, 26-filtrate dnockout pipeline, 27-feed solution pipeline.
Embodiment
The utility model to be further elaborated by specific embodiment below in conjunction with accompanying drawing, be noted that for those skilled in the art, under the prerequisite not departing from the utility model principle, the application's claims limited range is all fallen within to the amendment of the various equivalent form of value of the present utility model.
Embodiment:
As shown in Figure 1, the treatment unit of a kind of high salinity high-COD waste water of the present utility model, comprise wastewater feed pump 10, distillation tower 1, sulfate crystal still 6 and toluene extraction tower 9, the outlet of described wastewater feed pump 10 is provided with wastewater feed pipeline 14, and be connected with described distillation tower 1 by described wastewater feed pipeline 14, described distillation tower 1 top is provided with gas phase discharge port, described gas phase discharge port is connected with overhead gas discharge pipe 15, described overhead gas discharge pipe 15 is connected with condenser 3, the gaseous phase outlet of described condenser 3 is connected with non-cold air discharge pipe 16, described non-cold air discharge pipe 16 is connected with vacuum system, condensate outlet is provided with bottom described condenser 3, described condensate outlet is connected with phlegma discharge pipe 19, described phlegma discharge pipe 19 is connected with distillation wastewater collection tank 5, discharge gate is provided with bottom described distillation tower 1, described discharge gate is connected with described sulfate crystal still 6 by pipeline, discharge port bottom described sulfate crystal still 6 is connected with crystallization kettle discharge pipe 23, described crystallization kettle discharge pipe 23 is connected with separating centrifuge 7, described separating centrifuge 7 is connected with centrifugation filtrate discharge pipe 25, described centrifugation filtrate discharge pipe 25 is connected with filtrate surge tank 8, discharge port bottom described filtrate surge tank 8 is connected with filtrate dnockout pipeline 26, described filtrate dnockout pipeline 26 is connected with filtrate dnockout pump 13, the outlet of described filtrate dnockout pump 13 is connected with feed solution pipeline 27, described feed solution pipeline 27 is connected with described toluene extraction tower 9, extraction wastewater discharge port is provided with bottom described toluene extraction tower 9, described extraction wastewater discharge port is connected with sink drainage.
Be provided with column plate in described distillation tower 1 tower, be provided with reboiler 2 outside tower, described reboiler 2 is provided with steam inlet and water of condensation discharge port.
Described vacuum system comprises vacuum buffer tank 4 and vacuum pump 11, described vacuum buffer tank 4 is connected with the gaseous phase outlet of described condenser 3 by described non-cold air discharge pipe 16, described vacuum buffer tank 4 top is provided with gaseous phase outlet, described gaseous phase outlet is connected with vacuum pipe 17, described vacuum pipe 17 is connected with described vacuum pump 11, phlegma discharge port is provided with bottom described vacuum buffer tank 4, described phlegma discharge port is connected with vacuum buffer tank phlegma discharge pipe 18, described vacuum buffer tank phlegma discharge pipe 18 and described phlegma discharge pipe 19 merge and are connected to described distillation wastewater collection tank 5.
The end socket of described condenser 3 is provided with refrigerated water import and the outlet of refrigerated water backwater.
Described distillation tower 1 bottom discharging mouth is connected with distillation residue discharge pipe 21, described distillation residue discharge pipe 21 is connected with distillation residue dnockout pump 12, the outlet of described distillation residue dnockout pump 12 is connected with crystallization kettle feed pipe 22, and described crystallization kettle feed pipe 22 is connected with described sulfate crystal still 6 top.
Described sulfate crystal still 6 inside is provided with mechanical stirring, and at the bottom of the still of described sulfate crystal still 6 and still top is respectively equipped with refrigerated water import and the outlet of refrigerated water backwater, adopts the cooling of refrigerated water inner coil pipe.
Described separating centrifuge 7 inside has been provided with water wash system, described water wash system is connected with washing water pipeline 20, the distillation phlegma that described washing water pipeline 20 obtains by carrying out through described distillation tower 1 and condenser 3 distilling, after condensation causes described separating centrifuge 7, and described separating centrifuge 7 is provided with sodium sulfate drainage line 24.
Described toluene extraction tower 9 middle and upper part is provided with wastewater feed mouth, is provided with toluene feed mouth in middle and lower part.Extracting toluene discharge port is provided with at top.
Working process of the present utility model is as follows:
First, pending waste water enters into distillation tower 1 by wastewater feed pump 10, then reboiler 2 pairs of distillation towers 1 heat, distillation tower 1 pair of waste water carries out underpressure distillation, in still-process, some low salts, the waste steam of low COD enters into condenser 3 from the top of distillation tower 1 from overhead gas discharge pipe 15 and carries out condensation cooling, the gas be not condensed enters into vacuum buffer tank 4, distillation wastewater collection tank 5 is entered into through vacuum buffer tank phlegma discharge pipe 18 again after part gas cooling in vacuum buffer tank 4, the cooled waste water of condenser 3 also enters into distillation wastewater collection tank 5 from phlegma discharge pipe 19, distillation wastewater collection tank 5 is for storing the waste water phlegma after distillation, in distillation tower 1, after distillation, remaining distillation residue are introduced into distillation residue dnockout pump 12 by distillation residue discharge pipe 21, enter into sulfate crystal still 6 by crystallization kettle feed pipe 22 again and carry out crystallisation by cooling, sodium sulfate crystal after crystallization enters into separating centrifuge 7 by crystallization kettle discharge pipe 23 and washs with washing water, then solid-liquid two-phase carries out centrifugation, the sodium sulfate crystal that namely solid phase is recovered to is discharged by sodium sulfate drainage line 24 and is collected, liquid phase enters into filtrate surge tank 8 by centrifugation filtrate discharge pipe 25, and then enter into filtrate dnockout pump 13 through filtrate dnockout pipeline 26, enter into extraction tower 9 finally by feed solution pipeline 27 and carry out extracting and separating by toluene, aqueous phase after extraction, salinity and the COD of the inside are lower, then just can be drained into Sewage treatment systems to process, incipient so high salinity, namely high-COD waste water processes completely.
By above-described embodiment, the salinity in waste water and COD can well be removed, avoid the dilution of follow-up workshop section to waste water, eliminate high salt high-COD waste water to the impact of biochemical system.And the distillation phlegma salinity that underpressure distillation produces is low, and COD content is low, can be applicable to the dissolving in producing and bath water.
The present embodiment is by the crystallization treatment to distillation residue, and can reclaim the sodium sulfate higher than 95% in waste water, after recrystallization, sodium sulfate purity is higher than 98%, can be used as industrial sulphuric acid sodium and uses.
Wastewater Treatment result after being processed by device of the present utility model is as shown in the table:
Table 1
| ? | Reducing waste water | Distillation waste water | Waste water after extraction |
| COD mg/L | 17000-21000 | 600-1500 | 3000-6000 |
| Salinity % | 25-35 | ＜0.5 | ＜5 |
Claims (8)
1. the treatment unit of one kind high salinity high-COD waste water, it is characterized in that: comprise wastewater feed pump (10), distillation tower (1), sulfate crystal still (6) and toluene extraction tower (9), the outlet of described wastewater feed pump (10) is provided with wastewater feed pipeline (14), and be connected with described distillation tower (1) by described wastewater feed pipeline (14), described distillation tower (1) top is provided with gas phase discharge port, described gas phase discharge port is connected with overhead gas discharge pipe (15), described overhead gas discharge pipe (15) is connected with condenser (3), the gaseous phase outlet of described condenser (3) is connected with non-cold air discharge pipe (16), described non-cold air discharge pipe (16) is connected with vacuum system, described condenser (3) bottom is provided with condensate outlet, described condensate outlet is connected with phlegma discharge pipe (19), described phlegma discharge pipe (19) is connected with distillation wastewater collection tank (5), described distillation tower (1) bottom is provided with discharge gate, described discharge gate is connected with described sulfate crystal still (6) by pipeline, the discharge port of described sulfate crystal still (6) bottom is connected with crystallization kettle discharge pipe (23), described crystallization kettle discharge pipe (23) is connected with separating centrifuge (7), described separating centrifuge (7) is connected with centrifugation filtrate discharge pipe (25), described centrifugation filtrate discharge pipe (25) is connected with filtrate surge tank (8), the discharge port of described filtrate surge tank (8) bottom is connected with filtrate dnockout pipeline (26), described filtrate dnockout pipeline (26) is connected with filtrate dnockout pump (13), the outlet of described filtrate dnockout pump (13) is connected with feed solution pipeline (27), described feed solution pipeline (27) is connected with described toluene extraction tower (9), described toluene extraction tower (9) bottom is provided with extraction wastewater discharge port, described extraction wastewater discharge port is connected with Sewage treatment systems.
2. the treatment unit of high salinity high-COD waste water according to claim 1, is characterized in that: be provided with column plate in described distillation tower (1) tower, be provided with reboiler (2) outside tower, described reboiler (2) is provided with steam inlet and water of condensation discharge port.
3. the treatment unit of high salinity high-COD waste water according to claim 1, it is characterized in that: described vacuum system comprises vacuum buffer tank (4) and vacuum pump (11), described vacuum buffer tank (4) is connected with the gaseous phase outlet of described condenser (3) by described non-cold air discharge pipe (16), described vacuum buffer tank (4) top is provided with gaseous phase outlet, described gaseous phase outlet is connected with vacuum pipe (17), described vacuum pipe (17) is connected with described vacuum pump (11), described vacuum buffer tank (4) bottom is provided with phlegma discharge port, described phlegma discharge port is connected with vacuum buffer tank phlegma discharge pipe (18), described vacuum buffer tank phlegma discharge pipe (18) and described phlegma discharge pipe (19) merge and are connected to described distillation wastewater collection tank (5).
4. the treatment unit of high salinity high-COD waste water according to claim 1, is characterized in that: the end socket of described condenser (3) is provided with refrigerated water import and the outlet of refrigerated water backwater.
5. the treatment unit of high salinity high-COD waste water according to claim 1, it is characterized in that: described distillation tower (1) bottom discharging mouth is connected with distillation residue discharge pipe (21), described distillation residue discharge pipe (21) is connected with distillation residue dnockout pump (12), the outlet of described distillation residue dnockout pump (12) is connected with crystallization kettle feed pipe (22), and described crystallization kettle feed pipe (22) is connected with described sulfate crystal still (6) top.
6. the treatment unit of high salinity high-COD waste water according to claim 1, it is characterized in that: described sulfate crystal still (6) inside is provided with mechanical stirring, at the bottom of the still of described sulfate crystal still (6) and still top is respectively equipped with refrigerated water import and the outlet of refrigerated water backwater, adopts the cooling of refrigerated water inner coil pipe.
7. the treatment unit of high salinity high-COD waste water according to claim 1, it is characterized in that: described separating centrifuge (7) inside is provided with water wash system, described water wash system is connected with washing water pipeline (20), the distillation phlegma that described washing water pipeline (20) obtains by carrying out through described distillation tower (1) and condenser (3) distilling, after condensation causes described separating centrifuge (7), and described separating centrifuge (7) is provided with sodium sulfate drainage line (24).
8. the treatment unit of high salinity high-COD waste water according to claim 1, is characterized in that: described toluene extraction tower (9) middle and upper part is provided with wastewater feed mouth, is provided with toluene feed mouth in middle and lower part; Extracting toluene discharge port is provided with at top.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105366746A (en) * | 2015-11-10 | 2016-03-02 | 唐山宝翔化工产品有限公司 | 2-naphthol wastewater processing technology |
| CN107879407A (en) * | 2017-12-26 | 2018-04-06 | 中农发河南农化有限公司 | A kind of recycling system for preparing ortho-aminotoluene and producing waste water |
| CN108773979A (en) * | 2018-06-28 | 2018-11-09 | 上海力脉环保设备有限公司 | A kind of Environmentally-frielow-energy-consumptipolycarboxylic low-energy-consumptipolycarboxylic tar refining processing method of sodium sulfate wastewater containing phenol |
| CN108821493A (en) * | 2018-06-28 | 2018-11-16 | 上海力脉环保设备有限公司 | A kind of Environmentally-frielow-energy-consumptipolycarboxylic low-energy-consumptipolycarboxylic tar refining processing method of sodium sulfate wastewater containing phenol |
| CN111704305A (en) * | 2020-07-14 | 2020-09-25 | 新乡瑞诺药业有限公司 | Wastewater recycling process and device |
| CN112279273A (en) * | 2019-07-24 | 2021-01-29 | 中国科学院过程工程研究所 | Treatment method for removing COD (chemical oxygen demand) of industrial byproduct salt |
| CN112279274A (en) * | 2019-07-25 | 2021-01-29 | 中国科学院过程工程研究所 | Method for removing COD (chemical oxygen demand) of industrial byproduct salt |
| CN114262110A (en) * | 2021-12-16 | 2022-04-01 | 湖南化工研究院有限公司 | Integrated synergic recovery method for sodium sulfate and methanol in wastewater from pirimiphos-methyl production |
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2014
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105366746A (en) * | 2015-11-10 | 2016-03-02 | 唐山宝翔化工产品有限公司 | 2-naphthol wastewater processing technology |
| CN107879407A (en) * | 2017-12-26 | 2018-04-06 | 中农发河南农化有限公司 | A kind of recycling system for preparing ortho-aminotoluene and producing waste water |
| CN108773979A (en) * | 2018-06-28 | 2018-11-09 | 上海力脉环保设备有限公司 | A kind of Environmentally-frielow-energy-consumptipolycarboxylic low-energy-consumptipolycarboxylic tar refining processing method of sodium sulfate wastewater containing phenol |
| CN108821493A (en) * | 2018-06-28 | 2018-11-16 | 上海力脉环保设备有限公司 | A kind of Environmentally-frielow-energy-consumptipolycarboxylic low-energy-consumptipolycarboxylic tar refining processing method of sodium sulfate wastewater containing phenol |
| CN108773979B (en) * | 2018-06-28 | 2021-06-29 | 上海力脉环保设备有限公司 | Environment-friendly low-energy-consumption treatment method for wastewater containing sodium phenolate refined from tar |
| CN112279273A (en) * | 2019-07-24 | 2021-01-29 | 中国科学院过程工程研究所 | Treatment method for removing COD (chemical oxygen demand) of industrial byproduct salt |
| CN112279274A (en) * | 2019-07-25 | 2021-01-29 | 中国科学院过程工程研究所 | Method for removing COD (chemical oxygen demand) of industrial byproduct salt |
| CN111704305A (en) * | 2020-07-14 | 2020-09-25 | 新乡瑞诺药业有限公司 | Wastewater recycling process and device |
| CN114262110A (en) * | 2021-12-16 | 2022-04-01 | 湖南化工研究院有限公司 | Integrated synergic recovery method for sodium sulfate and methanol in wastewater from pirimiphos-methyl production |
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