CN1644537A - Polyether polyatomic alcohol producing sewage recovering and utilizing treatment - Google Patents
Polyether polyatomic alcohol producing sewage recovering and utilizing treatment Download PDFInfo
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- CN1644537A CN1644537A CNA2004100939533A CN200410093953A CN1644537A CN 1644537 A CN1644537 A CN 1644537A CN A2004100939533 A CNA2004100939533 A CN A2004100939533A CN 200410093953 A CN200410093953 A CN 200410093953A CN 1644537 A CN1644537 A CN 1644537A
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- production waste
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- polyether glycol
- anaerobic reactor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
A treating process for recovering and utilizing polyether poly-alcohol production sewage is carried out by producing sewage, entering regulating pool, regulating pool connection with oil separated pool, batching pool, anaerobic reactor, oxygen contacting oxidizing pool and settling pool, clear liquid of settling pool self-flowing into light catalyst oxidizing reactor, the mud and the mud of anaerobic reactor entering into mud concentrating pool, entering into dewaterer, light catalyst oxidizing reactor connection with continuous super-filtering treater and reversing-penetrating treater, adding medicament into batching pool by medicine added box, and supplying oxygen for oxygen contacting oxidizing pool and light catalyst oxidizing reactor by fan. Its advantages include low cost and consumption, to decrease occupied area.
Description
Technical field
The present invention relates to sewage disposal and regeneration, is a kind of technology of processing of polyether glycol production waste recycling specifically.
Background technology
Polyether glycol is mainly used in the production urethane foam, also as suds-stabilizing agent, paper industry defoamer, crude oil demulsifier, high-effective low foam washing composition, lubricant, quenching medium, emulsion foaming agent, multiple cutting agent, rubber lubricant and dedicated solvent etc., its purposes is very extensive.Because polyether glycol itself and most of raw materials for production thereof all are the organism of extremely difficult degradation, so the extremely difficult processing of the sewage that is produced in the production process.Many producers directly discharge, and give to be received environment and cause huge pollution.In addition, along with the worsening shortages of water resources, problem of water saving more and more obtains people's common concern, many enterprises begin to adopt reuse of wastewater in order to reduce cost, especially chemical industry, the water of productive use amount is big, and this just makes recycling sewage generated by making seem more urgent.Because polyether glycol production waste pollutent is difficult to handle, also do not see at present the treatment process of relevant polyether glycol production waste recycling and the report of method, just report after some producer adopts the method for dilution to reduce organic concentration and use traditional Wastewater Treated by Activated Sludge Process again.
The subject matter that this method exists is: cause treatment capacity to increase with sanitary sewage diluting high-concentration factory effluent, running expense improves, and economic benefit reduces.In addition, organism major part contained in the sewage is the organism of difficult degradation, utilizes aerobic biological treatment to be difficult to remove, and the clearance of pollutent is very low.Sewage after the processing is difficult to reach emission standard, causes very big pollution to environment.Can not recycle sewage, cause huge water resource waste.
Summary of the invention
In order effectively to remove the organism of difficult degradation in the polyethers sewage, reach the standard of recirculated cooling water supplementary feed, the present invention proposes following technical scheme:
Production waste 1 at first enters equalizing tank 2, and equalizing tank 2 is connected with oil trap 3, dosing chamber 4, anaerobic reactor 5, aerobic contact oxidation pond 6 and settling tank 7 successively; The supernatant liquor gravity flow of settling tank 7 enters photocatalysis oxidation reaction device 8, and mud enters sludge thickener 12 together with the mud of anaerobic reactor, enters water trap 13 then; Photocatalysis oxidation reaction device 8 is connected with continuous ultrafiltration treater 9, and then is connected with reverse-osmosis treated device 10; Add medicament by dosing tank 14 to dosing chamber 4; Provide oxygen to aerobic contact-oxidation pool 6 and photocatalysis oxidation reaction device 8 respectively by blower fan 15; The biogas that anaerobic reactor 5 produces enters collecting methane device 16; Reuse water 11 is recycled.
What anaerobic treatment reactor 5 adopted is CGSB, and operating temperature is 30 ± 1 ℃.
Add in trace elements irons, cobalt, nickel, manganese, copper, zinc and the VITAMIN one or more by dosing tank 16, guarantee in the water outlet concentration at 0.01-0.1mg/l, and add continuously.。
The hydraulic detention time of anaerobic reactor 5 is 2 ~ 5 days.
By dosing tank 16 interpolation liquid caustic soda, sheet alkali composition all is the adjusting that NaOH carries out basicity, and the basicity that guarantees water outlet is at 1500-3000mg/l, and basicity is with CaCO
3Meter.
Photocatalysis oxidation reaction device 8, photocatalyst is a Nano titanium dioxide, above glass filler, utilizes ultraviolet lamp to shine simultaneously, the wavelength of ultraviolet lamp is chosen in the irradiation of the light of 270-300nm, and the oxygen that utilizes blower fan 15 to provide simultaneously carries out aeration.
Continuous ultrafiltration treater 9 adopts rolled membrane module, and recirculated water is back to photocatalysis oxidation reaction device 8 front portions, and percolation water is as the water inlet of reverse-osmosis treated device 10.The ultra-filtration membrane of 0.01 μ m is adopted in the aperture.
Flow into equalizing tank after the sewage of high density comes out from the workshop, finish the adjusting of water quality and quantity herein, utilize the lifting of sump pump to enter oil trap, remove the oil slick in the sewage; Sewage gravity flow subsequently enters dosing chamber, finishes the lifting of temperature and adding of nutritive element at this, utilizes submersible pump to promote and enters the anaeration in normal temperature reactor, and the biogas that the anaerobic degradation organism produces is as energy utilization.Anaerobic reactor water outlet gravity flow enters the aerobic contact oxidation pond, further removes organism.The water outlet of aerobic contact oxidation pond is carried out mud-water separation at settling tank.Supernatant liquor after the separation enters the photocatalysis oxidation reaction device, the water outlet of photocatalysis oxidation reaction device enters the continuous ultrafiltration treater, water after the filtration passes through the reverse-osmosis treated device again, and the effluent quality index reaches recirculated cooling water supplementary feed water quality standard, can recycle.The excess sludge of settling tank and the excess sludge of anaerobic reactor together enter sludge thickener, concentrate laggard water trap.
Anaerobic reactor adopts expanded granular sludge bed anaerobic reactor (EGSB), and volumetric loading can reach 10 ~ 20kgCOD/m
3.d.
Description of drawings
Fig. 1 is a process flow sheet of the present invention
Wherein: 1. production waste 2. equalizing tanks 3. oil traps 4. dosing chambers 5. anaerobic reactors 6. aerobic contact oxidation ponds 7. settling tanks, 8. photocatalysis oxidation reaction devices, 9. continuous ultrafiltration treaters, 10. reverse-osmosis treated devices, 11. reuse waters, 12. sludge thickeners, 13. water traps, 14. dosing tanks 15. blower fans 16. collecting methane devices
Beneficial effect of the present invention
1. cut down the consumption of energy
Because anaerobic reaction does not need aeration, can save a large amount of power consumptions; In addition the organism of the every degraded of anaerobic reactor 1kg will produce approximately contain 50～70% methane biogas 0.5m3, these gases can be used as the utilization of fine fuel; This technical process is simple, and used power-equipment is few than traditional method, can reduce the energy consumption of polyethers sewage disposal.
2. effectively remove hardly degraded organic substance in the sewage
Because organic degraded has been experienced hydrolysis, acidifying, product acid and has been produced the methane four-stage in anaerobic reactor.Like this for some as being difficult to the organism of being degraded and can becoming small-molecule substance or chain rupture is utilized by anaerobion of long-chain and band phenyl ring etc. by the acidication process by aerobic bacteria, improve the biological degradability of sewage.
Utilize strong oxidizing substance photochemical catalytic oxidation agent, further remove the residual organic substances in the sewage, these organism are materials that biological treatment is difficult to degrade, and can utilize the technology of photochemical catalytic oxidation effectively to remove.
3. reduce floor space and investment
The anaerobic reactor volumetric loading will be higher than aerobic reactor far away, and the anaerobic reactor organic loading can reach 10 ~ 20kgCOD/m3.d, and traditional activated sludge process generally has only 0.5kgCOD/m3.d, so just can reduce floor space.The present invention adopts state-of-the art in the world at present anaerobic reactor-expanded granular sludge bed anaerobic reactor, adopts brand-new design, has improved the efficient of reactor greatly.So, can reduce the residence time greatly, reduce floor space and reduce investment.
4. system's running is stable
Anaerobic reactor and contact oxidation technology that the present invention adopts have very high anti impulsion load, so have better anti-hitting property of punching method for the variation of water quality and quantity.There is not the restriction of sludge bulking phenomenon and dissolved oxygen in anaerobic reactor, for the steady running of whole technology provides guarantee.
5. effectively solving excess sludge handles problems
The surplus sludge volume of this technology will be far smaller than the sludge yield that traditional digester is handled excess sludge, and the excess sludge organic content also will be lower than digester, has reduced the possibility of mud secondary pollution.Finally like this will alleviate the risk of sludge treatment cost and secondary pollution greatly.
6. effectively solve the pollution problem of reverse osmosis
Through the sewage after the Treatment by Photocatalysis Oxidation, at first handle, not only can further remove the suspended substance in the sewage, alleviate the operating pressure of follow-up reverse-osmosis treated device through continuous ultrafiltration, reduce the backwash cycle of reverse osmosis, raise labour efficiency and save running cost.
Embodiment
Embodiment 1
After production waste 1 process equalizing tank 2 and the oil trap 3, enter rise to 30 ℃ of finishing temperature in the dosing chamber 4, and carry out the adjusting (basicity is counted 1500mg/l with CaCO3) of basicity by dosing tank 16, add microelement nickel, manganese, copper, zinc and each 0.05mg/l of VITAMIN, enter anaerobic reactor 5 degradation of organic substances then and be converted into biogas as energy utilization; The water outlet of anaerobic reactor 5 continues degradation of organic substances in aerobic contact oxidation pond 7, provide the aerobic contact oxidation pond needed oxygen by blower fan 15; Discharging enters photocatalysis oxidation reaction device 8 mud-water separation is carried out in the water outlet of aerobic contact oxidation reactor 7 in settling tank 8 after, the oxygen that utilizes blower fan 15 to provide simultaneously, the organism that utilizes strong oxidizing property degradation biological method to be difficult to degrade, the water outlet of photocatalysis oxidation reaction device 8 enters continuous ultrafiltration treater 9, remove suspended substance and part colloidal type compound in the water, water outlet enters reverse-osmosis treated device 10.Through the processing of reverse-osmosis treated device 10, water outlet 11 water quality can reach the standard of recirculated cooling water supplementary feed, can reuse.The excess sludge that anaerobic reactor 5 and settling tank 7 are produced enters and dewaters 13 after concentration basin 12 concentrates.
Anaerobic reactor adopts expanded granular sludge bed anaerobic reactor (EGSB), and volumetric loading is 15kgCOD/m3.d.
The operating temperature of anaerobic reactor 5 is 30 ± 1 ℃.
Carry out the adjusting of basicity by dosing tank 16 interpolation liquid caustic soda, sheet alkali (composition all is NaOH), the basicity that guarantees water outlet is at 1500-3000mg/l, and basicity is with CaCO
3Meter.
The hydraulic detention time of anaerobic reactor 5 is 3 days, guarantees some organic pollutants that are difficult to degrade acidication and methanation completely, guarantees clearance, and clearance reaches 71%.
The biogas that anaerobic reactor 5 is produced can be delivered to boiler, and burning utilizes.
Photocatalysis oxidation reaction device 8, photocatalyst is a Nano titanium dioxide, above glass filler, utilize ultraviolet lamp to shine simultaneously, the wavelength of ultraviolet lamp is chosen in the irradiation of the light of 280nm, and the oxygen that utilizes blower fan 15 to provide simultaneously carries out aeration, the oxidation capacity of reinforcement photocatalysis oxidation reaction device 8.
Continuous ultrafiltration treater 9 adopts rolled membrane module, and recirculated water is back to photocatalysis oxidation reaction device 8 front portions, continues to utilize photocatalysis oxidation reaction device 8 oxidations organism wherein, and percolation water is as the water inlet of reverse-osmosis treated device 10.The ultra-filtration membrane of 0.01 μ m is adopted in the aperture.
Salinity in the condensed water of reverse-osmosis treated device 10 contains a large amount of phosphoric acid salt, and these have good fertility, can be used for irrigating the meadow.
Water outlet 11 water-quality guideline of reverse-osmosis treated device 10 are recirculated cooling water supplementary feed standard, can recycle.
Claims (7)
1. the treatment process recycled of a polyether glycol production waste, it is characterized in that: production waste (1), at first enter equalizing tank (2), equalizing tank (2) is connected with oil trap (3), dosing chamber (4), anaerobic reactor (5), aerobic contact oxidation pond (6) and settling tank (7) successively; The supernatant liquor gravity flow of settling tank (7) enters photocatalysis oxidation reaction device (8), and mud enters sludge thickener (12) together with the mud of anaerobic reactor, enters water trap (13) then; Photocatalysis oxidation reaction device (8) is connected with continuous ultrafiltration treater (9), and then is connected with reverse-osmosis treated device (10); Add medicament by dosing tank (14) to dosing chamber (4); Provide oxygen to aerobic contact-oxidation pool (6) and photocatalysis oxidation reaction device (8) respectively by blower fan (15); The biogas that anaerobic reactor (5) produces enters collecting methane device (16); Reuse water (11) is recycled.
2. according to the treatment process of the described polyether glycol production waste recycling of claim 1, it is characterized in that: what anaerobic treatment reactor (5) adopted is CGSB, and operating temperature is 30 ± 1 ℃.
3. the treatment process of recycling according to the described polyether glycol production waste of claim 1, it is characterized in that: add in trace elements iron, cobalt, nickel, manganese, copper, zinc and the VITAMIN one or more by dosing tank (16), guarantee in the water outlet concentration at 0.01-0.1mg/l, and add continuously.
4. according to the treatment process of the described polyether glycol production waste recycling of claim 1, it is characterized in that: the hydraulic detention time of anaerobic reactor (5) is 2 ~ 5 days.
5. the treatment process of recycling according to the described polyether glycol production waste of claim 1, it is characterized in that: carry out the adjusting of basicity by dosing tank (16) interpolation liquid caustic soda, sheet alkali (composition all is NaOH), the basicity that guarantees water outlet is at 1500-3000mg/l, and basicity is with CaCO
3Meter.
6. the treatment process of recycling according to the described polyether glycol production waste of claim 1, it is characterized in that: photocatalysis oxidation reaction device (8), photocatalyst is a Nano titanium dioxide, above glass filler, utilize ultraviolet lamp to shine simultaneously, the wavelength of ultraviolet lamp is chosen in the irradiation of the light of 270-300nm, and the oxygen that utilizes blower fan (15) to provide simultaneously carries out aeration.
7. the treatment process of recycling according to the described polyether glycol production waste of claim 1, it is characterized in that: continuous ultrafiltration treater (9) adopts rolled membrane module, recirculated water is back to photocatalysis oxidation reaction device (8) front portion, and percolation water is as the water inlet of reverse-osmosis treated device (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100939533A CN100509661C (en) | 2004-12-16 | 2004-12-16 | Treating technique of polyether polyatomic alcohol producing sewage recovering and utilization |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100939533A CN100509661C (en) | 2004-12-16 | 2004-12-16 | Treating technique of polyether polyatomic alcohol producing sewage recovering and utilization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1644537A true CN1644537A (en) | 2005-07-27 |
| CN100509661C CN100509661C (en) | 2009-07-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100939533A Expired - Fee Related CN100509661C (en) | 2004-12-16 | 2004-12-16 | Treating technique of polyether polyatomic alcohol producing sewage recovering and utilization |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102372402A (en) * | 2011-10-09 | 2012-03-14 | 南京工业大学 | Treatment method of polyether polyol wastewater |
| CN101624246B (en) * | 2009-08-19 | 2012-09-26 | 中国海洋石油总公司 | Technology for treating and reusing sewerages of industrial circulating water |
| CN103288294A (en) * | 2013-05-07 | 2013-09-11 | 江苏长华聚氨酯科技有限公司 | Treatment method of polyether-containing wastewater |
| CN103288292A (en) * | 2013-05-07 | 2013-09-11 | 江苏长华聚氨酯科技有限公司 | Processing method for polyether-containing wastewater |
| CN103449661A (en) * | 2013-05-07 | 2013-12-18 | 江苏长华聚氨酯科技有限公司 | Method for treating polyether wastewater |
| CN105271590A (en) * | 2015-10-30 | 2016-01-27 | 中国石油天然气股份有限公司 | Treatment method of low-concentration methanol-containing wastewater in gas field |
| CN105417846A (en) * | 2015-11-13 | 2016-03-23 | 淄博正大聚氨酯有限公司 | Method for treating polyether polyol process wastewater |
| CN107352732A (en) * | 2016-05-10 | 2017-11-17 | 张振家 | A kind of wastewater from edible oil production processing system and processing method |
-
2004
- 2004-12-16 CN CNB2004100939533A patent/CN100509661C/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101624246B (en) * | 2009-08-19 | 2012-09-26 | 中国海洋石油总公司 | Technology for treating and reusing sewerages of industrial circulating water |
| CN102372402A (en) * | 2011-10-09 | 2012-03-14 | 南京工业大学 | Treatment method of polyether polyol wastewater |
| CN102372402B (en) * | 2011-10-09 | 2014-04-09 | 南京工业大学 | Treatment method of polyether polyol wastewater |
| CN103288294A (en) * | 2013-05-07 | 2013-09-11 | 江苏长华聚氨酯科技有限公司 | Treatment method of polyether-containing wastewater |
| CN103288292A (en) * | 2013-05-07 | 2013-09-11 | 江苏长华聚氨酯科技有限公司 | Processing method for polyether-containing wastewater |
| CN103449661A (en) * | 2013-05-07 | 2013-12-18 | 江苏长华聚氨酯科技有限公司 | Method for treating polyether wastewater |
| CN103288292B (en) * | 2013-05-07 | 2015-03-25 | 江苏长华聚氨酯科技有限公司 | Processing method for polyether-containing wastewater |
| CN103288294B (en) * | 2013-05-07 | 2015-03-25 | 江苏长华聚氨酯科技有限公司 | Treatment method of polyether-containing wastewater |
| CN103449661B (en) * | 2013-05-07 | 2015-04-08 | 江苏长华聚氨酯科技有限公司 | Method for treating polyether wastewater |
| CN105271590A (en) * | 2015-10-30 | 2016-01-27 | 中国石油天然气股份有限公司 | Treatment method of low-concentration methanol-containing wastewater in gas field |
| CN105417846A (en) * | 2015-11-13 | 2016-03-23 | 淄博正大聚氨酯有限公司 | Method for treating polyether polyol process wastewater |
| CN107352732A (en) * | 2016-05-10 | 2017-11-17 | 张振家 | A kind of wastewater from edible oil production processing system and processing method |
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| Publication number | Publication date |
|---|---|
| CN100509661C (en) | 2009-07-08 |
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Granted publication date: 20090708 Termination date: 20100118 |