CN107311370A - A kind of processing method of glycol production waste water - Google Patents
A kind of processing method of glycol production waste water Download PDFInfo
- Publication number
- CN107311370A CN107311370A CN201610264648.9A CN201610264648A CN107311370A CN 107311370 A CN107311370 A CN 107311370A CN 201610264648 A CN201610264648 A CN 201610264648A CN 107311370 A CN107311370 A CN 107311370A
- Authority
- CN
- China
- Prior art keywords
- waste water
- stripper
- production waste
- processing method
- glycol production
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
Abstract
The present invention relates to the processing method of glycol production waste water, comprise the following steps：The first step, oxalic acid ester process glycol production waste water is successively with after the water outlet of stripper tower reactor and the heating of stripper overhead steam indirect heat exchange, stripping processing is carried out into stripper；Second step, the pH of stripper water outlet is first adjusted to 2.0~4.5, then carry out high-temperature S removal processing to the stripper water outlet for having adjusted pH；3rd step, high-temperature S removal processing water outlet enters precipitation reactor, and the pH of precipitation reactor is adjusted to 6~9, with carry out soluble iron precipitation reaction and water in remain the decomposition of hydrogen peroxide；4th step, the precipitation mixture that the 3rd step is obtained carries out gravity settling separation or centrifugation, and the iron precipitate isolated can empty back into second step recycling.The content of Isosorbide-5-Nitrae dioxane can be reduced to below 1mg/L in method of the present invention, waste water, and COD can be down to below 80mg/L, and TOC can be down to below 40mg/L.
Description
Technical field
It is specifically a kind of difficult biological the present invention relates to a kind of processing method of organic chemical waste water
The processing method of degraded organic chemical waste water.What espespecially a kind of oxalic acid ester process production ethylene glycol was produced
The processing method of waste water.
Background technology
Ethylene glycol is a kind of important industrial chemicals and strategic materials, is that consumption figure is maximum in the world
Polyalcohol, available for manufacture polyester (can further produce terylene, beverage bottle, film), fried
Medicine, glyoxal, and antifreezing agent, plasticizer, hydraulic fluid and solvent etc. can be made.Traditional second two
Alcohol production is completely dependent on oil ethene route, and cost is high.Coal ethyl glycol technology is then with coal generation
For oil ethylene production ethylene glycol.Such technology path meets China's oil starvation, few gas, coal money
The resources characteristic of source relative abundance, with obvious economic benefit and social benefit.
Ethylene glycol is prepared by raw material of coal at present, mainly there are three process routes：
Direct method：With coal gasification producing synthesis gas (CO+H2), then it is direct by the step of synthesis gas one
Synthesizing glycol.The key of this technology is the selection of catalyst, considerably long in the period of in be difficult to
Realize industrialization.
2nd, olefin processes：Using coal as raw material, by obtaining synthesis gas after gasification, conversion, purification,
Through methanol-fueled CLC, methanol-to-olefins (MTO) obtain ethene, then through ethylene epoxidizing, ring
Oxidative ethane is hydrated and product purification, finally gives ethylene glycol.The process by coal-to-olefin with tradition
Petroleum path preparing ethylene glycol is combined, and technology is more ripe, but cost is of a relatively high.
3rd, oxalic acid ester process：Using coal as raw material, pass through gasification, conversion, purification and separating-purifying
After respectively obtain CO and H2, wherein CO, which is synthesized and refined by catalytic coupling, produces oxalate,
Pass through again and H2Carry out hydrogenation reaction and the process by obtaining polyester grade ethylene glycol after refining.Should
Technological process is short, and cost is low, is current country's degree of attracting attention highest coal-ethylene glycol technology.
Using oxalic acid ester process production technology, will be produced by producing ethylene glycol product per ton by 0.5~1.0 ton
Hc effluent, the waste water mainly dirt such as dioxane containing 1.4- (dioxanes), methanol, nitrate nitrogen
Contaminate thing, with salinity is high, difficult for biological degradation the features such as, wherein Organic Pollutants in Wastewater is main
It is that it is difficult to biodegradation based on 1.4- dioxane (dioxanes).
The processing method for the highly concentrated production waste water that ethylene glycol is produced is produced about oxalic acid ester process at present,
It yet there are no related specific report.
The content of the invention
For defect present in prior art, it is an object of the invention to provide a kind of ethylene glycol
The processing method of waste water is produced, COD, TOC and 1.4 2 of waste water can be effectively reduced
The content of the ring of oxygen six.
The water quality of meaning oxalic acid ester process glycol production waste water of the invention is as follows：COD in waste water
For 10000~20000mg/L, TOC is 3000~6000mg/L, belongs to a kind of highly concentrated organic
Waste water, the Organic Pollutants in Wastewater overwhelming majority is Isosorbide-5-Nitrae-dioxane, its content
2000-7000mg/L.Waste water BOD5/CODcrLess than 0.1, it is difficult to biodegradable.
To achieve the above objectives, the present invention is adopted the technical scheme that：
A kind of processing method of glycol production waste water, comprises the following steps：
The first step, glycol production waste water steams with the water outlet of stripper tower reactor and stripper overhead successively
After the heating of vapour indirect heat exchange, stripping processing is carried out into stripper,
Stripper overhead steam rich in 1,4 dioxane is recyclable after indirect heat exchange is cooled down
Or burning disposal.
The bottom temperature control of stripper is 102~120 DEG C, and the number of theoretical plate control of stripper is
10~20 pieces, the tower top discharge control of stripper is into the 10~20% of tower water.Stripper
Tower top pressure control be normal pressure.
Under the operating conditions described above, the content of 1.4 dioxane can be with the water outlet of stripper tower reactor
It is reduced within 200mg/L.Above-mentioned glycol production waste water is carried out using steam stripped method
Processing, can remove most Isosorbide-5-Nitrae-dioxane in waste water.
Second step, is first adjusted the pH of stripper water outlet to 2.0~4.5, it is therefore an objective to after ensuring
PH conditions required for continuous high-temperature S removal processing.Then to having adjusted pH stripper
Water outlet carries out high-temperature S removal processing, it is therefore an objective to remaining organic contamination in effective Decomposition Wastewater
Thing.
High-temperature S removal processing oxidant use mass fraction for 27.5% hydrogen peroxide, it is double
The consumption of oxygen water be every liter of waste water in add 5~10ml hydrogen peroxide.
The catalyst of high-temperature S removal processing uses water-soluble inorganic molysite, and the consumption of molysite is
Every liter of waste water adds 50~200mg Fe.
The temperature control of high-temperature S removal processing is 80~99 DEG C, and Stress control is normal pressure,
Reaction time or mean residence time control to be 10~90min.
3rd step, high-temperature S removal processing water outlet enters precipitation reactor, by precipitation reactor
PH adjust to 6~9, with carry out soluble iron precipitation reaction and water in remain hydrogen peroxide
Decomposition.
Reaction time control is 5~30min in 3rd step, and reaction temperature control is 80~99 DEG C,
Reaction pressure is normal pressure.
The purpose of 3rd step mainly has three：One is to ensure that wastewater pH meets qualified discharge requirement；
Two be allow solubilised state in waste water iron precipitation completely (solubilised state total iron content reach 1mg/L with
Under)；Three be to allow in waste water the H remained2O2Decompose complete.
After being operated by the 3rd step, if also remaining more H in waste water2O2If,
Following adverse effect will be produced：(1) follow-up settling operation is disturbed, because being sunk in follow-up
Drop in operating process, H2O2It may proceed to decompose, and produce bubble, if sticking to iron precipitation
On thing, the settling property for causing iron precipitate is deteriorated, so as to influence the recovery of iron precipitate；
(2) H present in waste water2O2COD can be contributed, waste water COD may be caused up to standard.
4th step, the precipitation mixture that the 3rd step is obtained carries out gravity settling separation or centrifugation point
From the iron precipitate isolated can empty back into second step recycling.
In this step, the temperature control of gravity settling separation or centrifugation is 60~90 DEG C,
The time control of gravity settling separation or centrifugation is 10~240min.
In the waste water that 4th step is isolated, content≤1mg/L of Isosorbide-5-Nitrae-dioxane, COD≤
80mg/L, TOC≤40mg/L.
A kind of processing method of glycol production waste water of the present invention, the wound of the technical program
The property made is mainly reflected in following two aspects：(1) stripping processing and high-temperature S removal are realized
The reasonable combination of processing, is handled the glycol production waste water using steam stripped method,
1.4 dioxane most in waste water are reclaimed；Reduce at subsequent high temperature catalysis oxidation
Oxidizer and reaction time needed for reason etc., and then reduce high-temperature S removal processing
Expense and investment；Complete organics removal is easier to simultaneously, subsequent wastewater treatment is effectively reduced
Pressure.Certainly, the glycol production waste water can't effectively be solved by relying solely on stripping processing
Qualified discharge problem, and high-temperature S removal processing can just solve strip processed waste water
The processing problem of middle remaining 1.4- dioxane.(2) temperature that the water outlet of stripper tower reactor has
Good temperature conditionss can be provided for subsequent high temperature catalytic oxidation treatment, inventor herein is led to
Cross research to find, under conditions of temperature is higher, high-temperature S removal handles 1.4 dioxane
Speed and depth be intended to be substantially better than the relatively low situation of temperature ratio.
Beneficial effects of the present invention：
Using the processing method of glycol production waste water of the present invention, in the waste water after processing
The content of Isosorbide-5-Nitrae-dioxane can be reduced to below 1mg/L, COD can be down to 80mg/L with
Under, TOC can be down to below 40mg/L.
Brief description of the drawings
The present invention has drawings described below：
The schematic flow sheet of Fig. 1 present invention.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing.
As shown in figure 1, a kind of processing method of glycol production waste water of the present invention, bag
Include following steps：
The first step, oxalic acid ester process glycol production waste water successively with the water outlet of stripper tower reactor and stripping
After the heating of column overhead steam indirect heat exchange, stripping processing is carried out into stripper, rich in Isosorbide-5-Nitrae two
The stripper overhead steam of the ring of oxygen six is recyclable after indirect heat exchange is cooled down or burning disposal.
The bottom temperature control of stripper is 102~120 DEG C, and the number of theoretical plate control of stripper is
10~20 pieces, the tower top discharge control of stripper is into the 10~20% of tower water.Stripper
Tower top pressure control be normal pressure.
Under the operating conditions described above, the content of 1.4 dioxane can be with the water outlet of stripper tower reactor
It is reduced within 200mg/L.Above-mentioned glycol production waste water is carried out using steam stripped method
Processing, can remove most Isosorbide-5-Nitrae-dioxane in waste water.
Second step, is first adjusted the pH of stripper water outlet to 2.0~4.5, it is therefore an objective to after ensuring
PH conditions required for continuous high-temperature S removal processing.Then to having adjusted pH stripper
Water outlet carries out high-temperature S removal processing, it is therefore an objective to remaining organic contamination in effective Decomposition Wastewater
Thing.
High-temperature S removal processing oxidant use mass fraction for 27.5% hydrogen peroxide, it is double
The consumption of oxygen water be every liter of waste water in add 5~10ml hydrogen peroxide.
The catalyst of high-temperature S removal processing uses water-soluble inorganic molysite, and the consumption of molysite is
Every liter of waste water adds 50~200mg Fe.
The temperature control of high-temperature S removal processing is 80~99 DEG C, and Stress control is normal pressure,
Reaction time or mean residence time control to be 10~90min.
3rd step, high-temperature S removal processing water outlet enters precipitation reactor, by precipitation reactor
PH adjust to 6~9, with carry out soluble iron precipitation reaction and water in remain hydrogen peroxide
Decomposition.
Reaction time control is 5~30min in 3rd step, and reaction temperature control is 80~99 DEG C,
Reaction pressure is normal pressure.
The purpose of 3rd step mainly has three：One is to ensure that wastewater pH meets qualified discharge requirement；
Two be allow solubilised state in waste water iron precipitation completely (solubilised state total iron content reach 1mg/L with
Under)；Three be to allow in waste water the H remained2O2Decompose complete.
After being operated by the 3rd step, if also remaining more H in waste water2O2If,
Following adverse effect will be produced：(1) follow-up settling operation is disturbed, because being sunk in follow-up
Drop in operating process, H2O2It may proceed to decompose, and produce bubble, if sticking to iron precipitation
On thing, the settling property for causing iron precipitate is deteriorated, so as to influence the recovery of iron precipitate；
(2) H present in waste water2O2COD can be contributed, waste water COD may be caused up to standard.
4th step, the precipitation mixture that the 3rd step is obtained enters separator and carries out gravitational settling point
From or centrifuge, the iron precipitate isolated can empty back into second step recycling.
In this step, the temperature control of gravity settling separation or centrifugation is 60~90 DEG C,
The time control of gravity settling separation or centrifugation is 10~240min.
In the waste water that 4th step is isolated, content≤1mg/L of Isosorbide-5-Nitrae-dioxane, COD≤
80mg/L, TOC≤40mg/L.
Embodiment 1
Certain company's oxalic acid ester process glycol production waste water, pH value is that 2.0, COD is 14000
Mg/L, TOC are 4000mg/L.1,4- dioxane contents 5000mg/L.Total nitrogen content
2000mg/L。
The control of stripper bottom temperature be 108 DEG C, stripper overhead Stress control be normal pressure,
Stripper number of theoretical plate is 15 pieces, stripper overhead discharge is condition into tower water 12%
Under, the content of dioxane drops within 120mg/L in stripper tower reactor water outlet.
Next, carrying out high-temperature S removal processing, the temperature of catalytic oxidation system to waste water
Degree control is 90 DEG C, pressure is that 3.0, total iron content is adjusted to alkali is 100 by normal pressure, pH
Mg/L, the consumption of 27.5% hydrogen peroxide are pressed and carried out per L waste water (water outlet of stripper tower reactor) 8ml
Add, reaction time control is 60min.
Next, being 90 DEG C, being with 30%NaOH solution regulation wastewater pH in wastewater temperature
20min is reacted under conditions of 7.0.
Next, carrying out gravity settling separation under conditions of wastewater temperature is 70 DEG C, separate
Time is 30min.
The content of Isosorbide-5-Nitrae-dioxane in prior art analysis waste water is used for 0.5mg/L, COD
For 65mg/L, TOC is 30mg/L.
Embodiment 2
Certain company's coal ethyl glycol production waste water, pH value is that 9.0, COD is 20000mg/L,
TOC is 6000mg/L.Isosorbide-5-Nitrae-dioxane content 7000mg/L, total nitrogen content 3000mg/L.
The control of stripper bottom temperature be 102 DEG C, stripper overhead Stress control be normal pressure,
Stripper number of theoretical plate is 10 pieces, stripper overhead discharge is condition into tower water 10%
Under, the content of dioxane drops within 200mg/L in stripper tower reactor water outlet.
Catalytic oxidation treatment is carried out to the waste water, the temperature control of catalytic oxidation system is
80 DEG C, pressure be that 4.5, total iron content is adjusted to sulfuric acid is 50mg/L, 27.5% by normal pressure, pH
The consumption of hydrogen peroxide, which is pressed, to be added, is reacted per L waste water (water outlet of stripper tower reactor) 10ml
Time control is 10min.
Next, being 80 DEG C, being 6.0 with NaOH solution regulation wastewater pH in wastewater temperature
Under conditions of react 5min.
Next, carrying out gravity settling separation under conditions of wastewater temperature is 60 DEG C, separate
Time is 10min.
The content 1mg/L, water outlet COD of Isosorbide-5-Nitrae-dioxane in waste water are analyzed using prior art
For 80mg/L, TOC is 40mg/L.
Embodiment 3
Certain company's coal ethyl glycol production waste water, pH value is that 9.0, COD is 10000mg/L,
TOC is 3000mg/L.Isosorbide-5-Nitrae-dioxane content 2000mg/L, total nitrogen content 1500mg/L.
The control of stripper bottom temperature be 120 DEG C, stripper overhead Stress control be normal pressure,
Stripper number of theoretical plate is 20 pieces, stripper overhead discharge is condition into tower water 20%
Under, the content of dioxane drops within 80mg/L in stripper tower reactor water outlet.
Catalytic oxidation treatment is carried out to the waste water, the temperature control of catalytic oxidation system is
99 DEG C, pressure be that 2.0, total iron content is adjusted to sulfuric acid is 200mg/L, 27.5% by normal pressure, pH
The consumption of hydrogen peroxide, which is pressed, to be added, is reacted per L waste water (water outlet of stripper tower reactor) 5ml
Time control is 90min.
Next, being 99 DEG C, being 9.0 with NaOH solution regulation wastewater pH in wastewater temperature
Under conditions of react 30min.
Next, carrying out gravity settling separation under conditions of wastewater temperature is 90 DEG C, separate
Time is 240min.
The content 1mg/L, water outlet COD of Isosorbide-5-Nitrae-dioxane in waste water are analyzed using prior art
For 60mg/L, TOC is 28mg/L.
The content not being described in detail in this specification belongs to known in professional and technical personnel in the field
Prior art.
Claims (18)
1. a kind of processing method of glycol production waste water, it is characterised in that including following step
Suddenly：
The first step, glycol production waste water steams with the water outlet of stripper tower reactor and stripper overhead successively
After the heating of vapour indirect heat exchange, stripping processing is carried out into stripper；
Second step, the pH of stripper water outlet is adjusted to 2.0~4.5, then to having adjusted pH
Stripper water outlet carry out high-temperature S removal processing；
3rd step, high-temperature S removal processing water outlet enters precipitation reactor, by precipitation reactor
PH adjust to 6~9, carry out the precipitation reaction of soluble iron and residual hydrogen peroxide in water
Decompose；
4th step, the precipitation mixture that the 3rd step is obtained carries out gravity settling separation or centrifugation point
From.
2. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The bottom temperature of stripper described in the first step is 102~120 DEG C, the tower top pressure of stripper
Power is normal pressure.
3. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The number of theoretical plate of stripper described in the first step is 10~20 pieces.
4. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The tower top discharge of stripper described in the first step is into the 10~20% of tower water.
5. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：Stripper overhead steam described in the first step is recyclable after indirect heat exchange is cooled down or burns
Processing.
6. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The content of 1,4 dioxane is reduced in the water outlet of stripper tower reactor after the first step is handled through stripping
To within 200mg/L.
7. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The oxidant of the processing of high-temperature S removal described in second step uses mass fraction for 27.5%
Hydrogen peroxide.
8. the processing method of glycol production waste water as claimed in claim 7, its feature exists
In：The consumption of the hydrogen peroxide be every liter of waste water in add 5~10ml hydrogen peroxide.
9. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The catalyst of the processing of high-temperature S removal described in second step uses water-soluble inorganic molysite.
10. the processing method of glycol production waste water as claimed in claim 9, its feature exists
In：The consumption of the water-soluble inorganic molysite is that every liter of waste water adds 50~200mg Fe.
11. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The temperature of the processing of high-temperature S removal described in second step is 80~99 DEG C, and pressure is normal
Pressure.
12. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The reaction time of the processing of high-temperature S removal described in second step is 10~90min.
13. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The temperature reacted described in 3rd step is 80~99 DEG C, and pressure is normal pressure.
14. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The time reacted described in 3rd step is 5~30min.
15. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The temperature of gravity settling separation or centrifugation described in 4th step is 60~90 DEG C.
16. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The time of gravity settling separation or centrifugation described in 4th step is 10~240min.
17. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：The iron precipitate that 4th step is isolated can be recycled.
18. the processing method of glycol production waste water as claimed in claim 1, its feature exists
In：4th step processing after effluent quality be：Content≤1mg/L of Isosorbide-5-Nitrae-dioxane, COD
≤ 80mg/L, TOC≤40mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610264648.9A CN107311370A (en) | 2016-04-26 | 2016-04-26 | A kind of processing method of glycol production waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610264648.9A CN107311370A (en) | 2016-04-26 | 2016-04-26 | A kind of processing method of glycol production waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107311370A true CN107311370A (en) | 2017-11-03 |
Family
ID=60185613
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610264648.9A Pending CN107311370A (en) | 2016-04-26 | 2016-04-26 | A kind of processing method of glycol production waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107311370A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5478857A (en) * | 1977-12-05 | 1979-06-23 | Kurita Water Ind Ltd | Appartus for treating water containing ammonia |
| CN101428865A (en) * | 2007-11-06 | 2009-05-13 | 大庆石油管理局 | Method for pretreatment of methanol industrial wastewater |
| CN102040302A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Treatment method of nitrochlorobenzene production wastewater |
| CN102050541A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Treatment method for wastewater from stripping tower |
| CN102417264A (en) * | 2010-09-28 | 2012-04-18 | 中国石油化工股份有限公司 | Method for treating nitrochlorobenzene production wastewater |
| CN103539300A (en) * | 2012-07-13 | 2014-01-29 | 中国石油化工股份有限公司 | Method for treating wastewater produced in preparation of butadiene through oxidative dehydrogenation of butylene |
| CN105084661A (en) * | 2015-08-12 | 2015-11-25 | 中石化炼化工程（集团）股份有限公司 | Coal-based ethylene glycol sewage treatment method and system |
-
2016
- 2016-04-26 CN CN201610264648.9A patent/CN107311370A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5478857A (en) * | 1977-12-05 | 1979-06-23 | Kurita Water Ind Ltd | Appartus for treating water containing ammonia |
| CN101428865A (en) * | 2007-11-06 | 2009-05-13 | 大庆石油管理局 | Method for pretreatment of methanol industrial wastewater |
| CN102040302A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Treatment method of nitrochlorobenzene production wastewater |
| CN102050541A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Treatment method for wastewater from stripping tower |
| CN102417264A (en) * | 2010-09-28 | 2012-04-18 | 中国石油化工股份有限公司 | Method for treating nitrochlorobenzene production wastewater |
| CN103539300A (en) * | 2012-07-13 | 2014-01-29 | 中国石油化工股份有限公司 | Method for treating wastewater produced in preparation of butadiene through oxidative dehydrogenation of butylene |
| CN105084661A (en) * | 2015-08-12 | 2015-11-25 | 中石化炼化工程（集团）股份有限公司 | Coal-based ethylene glycol sewage treatment method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Prabakar et al. | Pretreatment technologies for industrial effluents: Critical review on bioenergy production and environmental concerns | |
| CN101139118B (en) | Technique for processing wastewater containing methanol and dimethyl ether | |
| CN100548895C (en) | The sewage treatment process that contains methyl alcohol and dme | |
| CN104556571B (en) | Recycling treatment process and system for wastewater in Fischer-Tropsch synthesis reaction | |
| EP3865461B1 (en) | Method for treating production wastewater from preparation of propylene oxide with co-oxidation method | |
| Qi et al. | Partial oxidation treatment of waste polyvinyl chloride in critical water: Preparation of benzaldehyde/acetophenone and dechlorination | |
| CN106698785A (en) | Coal gasification wastewater phenol and ammonia recovery process | |
| CN103601616B (en) | Alcohol-water separation recycling method of Fischer-Tropsch synthesis reaction water | |
| CN108085039A (en) | A kind of method that biomass by hydro-thermal liquefaction bio oil is modified | |
| CN107311370A (en) | A kind of processing method of glycol production waste water | |
| CN107311338A (en) | A kind of processing method of glycol production waste water | |
| CN107311389A (en) | A kind of coal ethyl glycol produces the processing method of waste water | |
| CN103833190B (en) | A kind of method and system of two-stage sludge processing | |
| CN102173522B (en) | Treatment and recycling process for initiator CH335 wastewater | |
| CN103663826B (en) | A kind of pretreatment process of HTS factory effluent | |
| CN210974476U (en) | Device for purifying acetic acid from acetic acid-containing wastewater | |
| CN102617309A (en) | Process for preparing acetaldehyde | |
| CN101260031B (en) | Method for preparing low-grade aliphatic acid from benzene and its homologues waste water | |
| CN213537769U (en) | Sewage system of acrolein continuous production 1, 3-propylene glycol technology | |
| CN107311388A (en) | A kind of coal ethyl glycol produces the processing method of waste water | |
| JPH08245485A (en) | Production of isophorone | |
| KR100403121B1 (en) | Process for separately preparing liquefied carbon dioxide, methane gas and byproducts from waste gas | |
| CN105776707A (en) | Method for treating metronidazole wastewater | |
| CN113307732A (en) | Synthetic method of plastic degradation recovery monomer | |
| CN113371881A (en) | Treatment method of process wastewater generated in one-step synthesis of N-phenylmaleimide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20171103 |