CN101475293A - Wastewater treating and recycling process - Google Patents
Wastewater treating and recycling process Download PDFInfo
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- CN101475293A CN101475293A CNA2009100779471A CN200910077947A CN101475293A CN 101475293 A CN101475293 A CN 101475293A CN A2009100779471 A CNA2009100779471 A CN A2009100779471A CN 200910077947 A CN200910077947 A CN 200910077947A CN 101475293 A CN101475293 A CN 101475293A
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Abstract
The invention relates to a method for treating dimethyl ether production waste water, which comprises the following main steps: after the dimethyl ether production waste water is treated through oil removal, carrying out secondary biochemical treatment successively, and then filtering, sterilizing and recycling the supernatant fluid for production after coagulating sedimentation. By adopting a running mode of connecting biochemical treatment units in series, the method ensures high quality of yielding water.
Description
Technical field
The invention belongs to technical field of waste water processing, be that a kind of methanol vapor phase solid catalyst that is used for is produced the treatment process that the production wastewater treatment of dme generation is back to industrial cooling circulating water make up water, also can be used for the Treatment for Reuse and the advanced treatment of similar sewage.
Background technology
A resource utilization that important development trend is exactly waste water of wastewater treatment, shortage of water resources is a secular problem, the water resources of China was just in short supply originally, along with expanding economy, demand to water is increasing, with wastewater treatment and renovation is the only way of alleviating the water resources anxiety, the waste water recycling standard is higher than general emission standard, " Code for design of industrial recirculating cooling water treatment " GB50050-2007 of the up-to-date promulgation of country has proposed clear and definite requirement to reuse water as the make up water of cooling circulating water, wherein COD requires less than 30mg/l, (Biochemical Oxygen Demand BOD) requires less than 5mg/l biological oxygen demand.
It is a stern challenge that existing sewage biochemical processing process will reach this standard, require under the very low situation of COD, BOD in water outlet, the design loading of biochemical device will be very low, biochemical device is also just very big, the investment that brings and take up an area of all increases, and if whole biochemical treatment system be in for a long time that operation also can be to the very big influence of steady running generation of system under the ultralow load.Adopt common biochemical treatment must increase multiple materialization processing (comprising technology such as coagulating sedimentation, filtration, advanced oxidation and activated carbon adsorption) and just can reach the reuse requirement, therefore complex treatment process, long flow path, cause investment excessive, running cost is too high.
Existing wastewater biochemical treatment technology is under the situation that satisfies different processing requirements, applicable scope is all arranged separately, the target of wastewater treatment in the past mostly is to be main purpose to satisfy qualified discharge, therefore the difference of various technology is not too big, existing biochemical treatment process for wastewater mainly is various activated sludge processes and various biomembrance process, as: conventional activated sludge process, A
2/ O method, oxidation ditch process, sequence intermittent activated sludge process (Sequencing Batch Activated Sludge Process, SBR) all there are the problem that floor space is big, the processing load is low, operation energy consumption is high in technology such as technology, bio-contact oxidation technology, BAF, these technologies.Current country advocates the wastewater treatment regeneration energetically, particularly reuse water has proposed higher processing requirements in the reuse of industrial circle to regeneration water quality, the method that the processing of waste water COD is most economical is still removed by the mode of biochemical treatment, any method by increase materialization processing links removal COD all is uneconomic, but existing treatment technology technology will drop to COD very low level, and it handles that load is lower, hydraulic detention time is longer, this will inevitably increase the cost of engineering, also is uneconomic.
It also is the problem that current ten minutes is paid close attention to that wastewater biochemical is handled energy-conservation, and conventional activated sludge process all needs special second pond to carry out mud-water separation and mud refluxing unit, and this can increase occupation of land and construction cost, and the backflow of mud needs power consumption, has increased working cost; Though SBR technology does not have mud to reflux and special second pond, biochemistry pool is intermittent operation, and the utilising efficiency of biochemistry pool is low also to be an important defective.
Dme is not only a kind of important chemical material (can be used for the synthetic of many fine chemicals), and is a kind of clean fuel and fuel dope; Also can be used as the intermediate of gasoline and alkene; In pharmacy, the purposes of many uniquenesses is arranged in the chemical industry such as agricultural chemicals; Can substitute chloro-fluoro-carbon kind (being the CFC material) as aerosol jet and refrigeration agent; Highly purified dme can be used as narcotic; In addition, dme can also become the surrogate of town gas and liquefied gas, also can be used as automobile fuel.Along with the aggravation of energy shortage problem, dme is as a kind of novel energy of instead of natural gas, and the demand in market is increasing, and dme manufacturer is also more and more, and the wastewater treatment that the dme production that thereupon brings is produced also becomes hot issue.
The water quality situation of dimethyl ether production wastewater is different and don't same because of the process for preparing dimethyl ether method, and its chemical oxygen demand (COD) (Chemical Oxygen Demand, variation range COD) is between hundreds of-several thousand mg/l, and the water yield is more or less the same.Present main treatment situation is to reach enterprise's emission standard based on processing, because differing greatly of water quality, thereby the processing technology routine of wastewater treatment is also different, data from report, major part all is to adopt biologic treating technique, different, main treatment technology combination according to raw water quality and processing target: anaerobic biological treatment+aerobe treatment technology is arranged to reach the mark emission standard, this technology is primarily aimed at the processing of high-concentration waste water.And acidication+catalytic oxidation technology+BAF then is fit to the dimethyl ether waste water processing of middle lower concentration to reach the technology of emission standard.
At present unique case of handling the technology report that is back to industrial cooling circulating water make up water about dimethyl ether production wastewater is to propose at the waste water characteristic that the compound sour catalytic dehydration of liquid phase method is produced dme technology, the waste water characteristic of this production technique is a pH value slant acidity, and COD is more than 3000mg/l.Though this technology also is to handle dimethyl ether production wastewater, the process for preparing dimethyl ether difference, the waste water characteristic of generation differs greatly.
Summary of the invention
The present invention mainly is the processing reuse of producing the factory effluent of dme at the methanol vapor phase catalytic dehydration, promptly the object of the present invention is to provide a kind of waste water treating and reutilizing of dimethyl ether production wastewater processing and technology of advanced treatment of wastewater of comprising, adopt the mode of biochemical treatment units in series to move, guaranteed high quality of yielding water.
For achieving the above object, dimethyl ether production wastewater provided by the invention is handled reuse technology, and its key step is:
Dimethyl ether production wastewater or sanitary wastewater after oil removal is handled, are successively entered first step biochemical reactor and second stage biochemical reactor carries out secondary biochemical treatment, and its supernatant liquor carries out filter-sterilized and is back to production behind coagulating sedimentation.
Be added with swash plate or inclined tube filler in the oil trap of the present invention, the residence time control of waste water is about 0.5～2 hour, and this oil trap can be circle and rectangular configuration, can be that steel, PVC, glass reinforced plastic or concrete cast-in-situ are built.
The biochemical reactor that the present invention adopts is that the gas-liquid-solid three-phase disjoint set is formed in biochemical reactor inside, and biochemical reactor integral body of the present invention is a container, and its inside is filled with active sludge or flowable biologic packing material carrier.Can adopt the biochemical reactor of following structure, its inside of this biochemical reactor includes:
The swash plate disengaging zone, surrounded by the settling region dividing plate, perhaps the sidewall by settling region dividing plate and biochemical device surrounds, and this swash plate disengaging zone can be positioned at the middle section of biochemical reaction device, also can be positioned at a side of biochemical reaction device, perhaps be positioned at the periphery of biochemical reaction device;
Biochemical reaction device can be circle, rectangle or gallery formula structure;
The aerobic aeration district, removing settling region dividing plate and reflux guide plate institute area surrounded space in addition in biochemical reaction device is the aerobic aeration district all.
Biochemical treatment apparatus inside is provided with reflux guide plate in the one or both sides of swash plate disengaging zone, forms a mixed-liquor return district; The upper end of this reflux guide plate is lower than the water surface in aerobic aeration district, and the lower end of this reflux guide plate is provided with mixed-liquor return seam and is communicated with the aerobic aeration district;
Between reflux guide plate and the biochemical treatment apparatus sidewall, the below of swash plate disengaging zone is provided with a mud and separates plate, forms a mud enrichment region; The upper end that this mud separates plate is higher than the water surface in aerobic aeration district, and the lower end that this mud separates plate is provided with the mud seam that refluxes and is communicated with the aerobic aeration district; This mud refluxes to stitch and stitches corresponding to mixed-liquor return.
On mud enrichment region top is the swash plate disengaging zone, the top of this swash plate disengaging zone forms a clear water zone, is positioned at this clear water zone and is provided with the water outlet captation, and this captation can be the overflow weir form, also can be the form of subduction water outlet, the design of subduction effluent adopting symmetry reversed return type.Referring to the water collector synoptic diagram.The water of each inlet enters and all passes through identical path behind the water collector and leave biochemical reaction device.
The bottom of biochemical treatment apparatus is provided with aerator, and this aerator connects an inlet pipe.
After the present invention handled by Two-Stage Biochemical, the factory effluent of its processing guaranteed that COD is controlled at below the 30mg/l.
Two-Stage Biochemical handle basic on, adopt the filtering common process of coagulating sedimentation (known technology), the turbidity that can guarantee treating water satisfies " Code for design of industrial recirculating cooling water treatment " GB50050-2007 fully to the requirement of reuse water as the make up water of cooling circulating water below 5 degree.Whole biochemical treatment system can keep the high processing load, and the COD of intaking immediately constantly changes, and final outflow water also can satisfy the strict demand of reuse standard all the time, and investment is suitable than conventional intermediate water reuse system.
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
Fig. 2 is a biochemical reactor structural representation of the present invention;
Fig. 3 is the connection diagram of biochemical reactor of the present invention when series connection is used
Fig. 4 is provided with the oil trap structural representation of swash plate or inclined tube filler for the present invention.
Embodiment
See also Fig. 1; technical process of the present invention is: factory effluent 21 at first enters the side reaction product that oil trap 22 is removed some similar oils; protect follow-up biochemical treatment system; waste water relies on gravity to enter first biochemical reactor 23; utilize the active sludge of first biochemical reactor, 23 middle and high concentrations to remove most organism,, former glassware for drinking water is had stronger impact resistance because sludge quantity is big; the sludge activity of self-circulation is better, and sludge loading is higher.Water outlet through after 23 processing of first biochemical reactor relies on gravity to enter second biochemical reactor 24.In this second biochemical reactor 24, microorganism on its active sludge or the bio-carrier (as: bioactive carbon, flyash or the like) is in poor nutritional status, and sludge loading is low than the last period, and sludge settling property is good, water quality is limpid, and the COD of this section can stably maintain below the 30mg/l.Water outlet after second biochemical reactor 24 is handled has the colloid and the suspended substance of trace, rise to coagulative precipitation tank 26 by lift pump 25 and carry out precipitation process, after sterilization pool 27 is handled after filtration with the supernatant liquor of post precipitation, below processing to 5 degree with the turbidity of water, reach processing requirements for production reuse 28.
The present invention uses two identical first biochemical reactor 13 and 14 series connection of second biochemical reactor of structure, and promptly the water outlet of first biochemical reactor is connected to the water-in of second biochemical reactor.Because first biochemical reactor of the present invention is identical with the structure of second biochemical reactor, therefore one of them is only described.
See also Fig. 2, be the structural representation of biochemical reactor of the present invention.
The middle part of biochemical reactor is aerobic aeration district 2; The lopsidedness ground of biochemical reactor inside forms a mixed-liquor return district 3 to having a reflux guide plate 10.This reflux guide plate 10 can adopt steel, PVC, ABS, glass reinforced plastic or concrete placement to form.The upper end of this dividing plate is lower than the upper end in aerobic aeration district 2, and the lower end of this reflux guide plate 10 is provided with mixed-liquor return seam 11 and is communicated with aerobic aeration district 2, and the generation mixed solution circulates during the assurance aeration.
Between the sidewall of reflux guide plate 10 and biochemical reactor 1, inclination down is provided with a mud and separates plate 7, forms a mud enrichment region 6; This mud separates plate 7 and can adopt steel, PVC, ABS, glass reinforced plastic or concrete placement to form.The upper end that this mud separates plate 7 is higher than the upper end in aerobic aeration district 2, and the lower end that this mud separates plate 7 has reflux seam 8 of a mud to be communicated with aerobic aeration district 2, and on being provided with, this mud refluxes and stitches 8 and stitch 11 corresponding to mixed-liquor return.
There is a solid-liquid displacement zone 5 mud enrichment region 6 tops, this solid-liquid displacement zone 5 is equipped with swash plate or inclined tube filler, mud dividing plate 7 is become two portions with spatial isolation between the biochemical reactor sidewall, and the top of solid-liquid displacement zone 5 is a clear water zone 4, and the top that is positioned at this clear water zone 4 is provided with water outlet; The water outlet of clear water zone 4 is catchmented and is adopted overflow weir or submerged water gathering system (this is not described in detail for known technology).The below of solid-liquid displacement zone 5 is a mud enrichment region 6.Clear water zone 4 and solid-liquid displacement zone 5 are isolated by settling region dividing plate 9 and aeration zone, and the bottom in the bottom of mud enrichment region 6 and mixed-liquor return district 3 is communicated with aerobic aeration district 2, but get back in the aerobic aeration district 2 for ease of active sludge or flowing carrier, below corresponding mud backflow seam 8 and mixed-liquor return seam 11, locate to be provided with obliquely slip plate 13.
The bottom of biochemical reactor 1 is provided with aerator 12, and this aerator 12 connects an inlet pipe.The aeration form can be micro-hole aerator, micropore aeration pipe or perforated pipe (this is known technology, is not described in detail).
Process when biochemical reactor of the present invention carries out wastewater treatment is, waste water enters the aerobic aeration district 2 of biochemical reactor 1, under the aeration effect of aerator 12, to intake rapidly with biochemical reactor 1 in the active sludge bio-carrier that maybe can flow mix fully, obtain containing maybe can the flow mixed solution of bio-carrier of active sludge, aerator 12 oxygenations in water simultaneously, because the effect at reflux guide plate 10 1 side aerations has produced density difference, cause mixed solution to flow in the both sides of reflux guide plate 10 automated cycle, further strengthened the mixing effect of water inlet and mixed solution, because return velocity is very fast, mixed-liquor return district 3 has kept good good oxygen condition, so this zone remains the effective area in aerobic aeration district, mixed-liquor return district 3 has gas-liquid separating function.Under the water level differential pressure action of water inlet water outlet, the mixed solution in aerobic aeration district enters mud enrichment region 6 by mud backflow seam 8, then mixed solution carries out solid-liquid separation in solid-liquid displacement zone 5, active sludge is retained in mud enrichment region 6, under action of gravity, turn back to mixed-liquor return district 3 by mud backflow seam 8, the mixed solution that refluxes will stitch 11 by mixed-liquor return from the mud of mud enrichment region 6, turn back to the aeration zone under the guide functions of slip plate.Solid-liquid displacement zone 5 is equipped with swash plate or inclined tube filler.And the water after handling is by solid-liquid displacement zone 5, water gathering system 14 water outlets that enter clear water zone 4.When waste water needed multiple-stage treatment, supernatant liquor entered the next stage biochemical treatment equipment by water gathering system 14.
The oil trap that the present invention adopts, its structure as shown in Figure 4, be that filler 43 is seated in the oil trap, waste water enters oil trap by water inlet pipe 48, waste water is under the water distribution effect of baffle device for water 41, top from filler 43 flows to packing layer equably, oil slick in the waste water becomes the surface that floats to oil trap on the bigger elaioleucite under the poly-effect of the prisoner of filler 43, waste water after the oil removing enters communicating pipe 46 from the hypomere outflow of filler 43, discharge by water outlet 45 with the water outlet of control oil trap by the elevation of water surface that goes out in the water regulating valve 44 adjusting oil traps, the oil slick of oil trap is discharged by oil discharge outlet 42, the bottom offers a sewage draining exit 49 in the oil trap, is used to get rid of the dirt in the oil trap.Filler 43 can be the form of swash plate or inclined tube, and material is hydrophobic lipophilic material.The design surface load of oil trap is 0.5～3 cubic metre/hour.
The gravity method filter tank that the multilayer filtrate is adopted in filter-sterilized of the present invention pond 7, also can adopt filtering under pressure, filtering filtering velocity is controlled at 3～8 meters/hour, this filter-sterilized pond 7 can be circle and rectangular configuration, can be that steel, PVC, glass reinforced plastic or concrete cast-in-situ are built (known technology is not recommended accompanying drawing).
Biochemical processing process of the present invention; mainly be that biochemical reactor (as shown in Figure 3) is used in series connection, waste water is carried out stage treatment, do not increase the lift technique of mud backflow and water again; not increasing construction investment, not making under the complicated prerequisite of flow process, guarantee to obtain high-quality effluent quality.
Adopt method of the present invention, with dimethyl ether production wastewater through each processing unit after final processing, its leading indicator data are as shown in table 1:
Table 1
| Water-quality guideline | Influent quality | One-level biochemistry | Secondary biochemical | Coagulating sedimentation filters |
| COD(mg/L) | 289 | 48.28 | 14.36 | 8 |
| pH | 7 | 7 | 7 | 7 |
| Turbidity (degree) | 4.6 | 0.7 |
All the other indexs also all satisfy " Code for design of industrial recirculating cooling water treatment " GB50050-2007 to the index request of reuse water as the cooling circulating water make up water.
Claims (6)
1, a kind of wastewater treatment and renovation method, its key step is:
Waste water after oil removal is handled, is successively carried out secondary biochemical treatment, and its supernatant liquor carries out filter-sterilized and is back to production behind coagulating sedimentation.
2, the method for claim 1, wherein waste water is 0.5～2 hour in the time that oil removal is handled.
3, the method for claim 1, wherein the waste water filtering velocity of carrying out filter-sterilized is controlled at 3～8 meters/hour.
4, every grade of biochemical treatment all has solid-liquid separation unit in the method for claim 1, wherein described secondary biochemical treatment.
5, between the method for claim 1, wherein described secondary biochemical treatment unit and biochemical treatment water outlet gravity enter biochemical treatment unit, the second stage.
6, the method for claim 1, wherein the unitary microorganism feature of one-level biochemical treatment is to be to purify main body with the bacterium, and the secondary biochemical treatment unit is to serve as to purify main body with bacterium, protozoon and metazoan.
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| CN 200910077947 CN101475293B (en) | 2009-02-04 | 2009-02-04 | Wastewater treating and recycling process |
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| CN101475293B CN101475293B (en) | 2013-09-25 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104860473A (en) * | 2015-05-08 | 2015-08-26 | 昆明理工大学 | Urban wastewater treatment system |
| CN105152498A (en) * | 2015-10-26 | 2015-12-16 | 河海大学 | Fish-gill-type oxygen-carrying purification system capable of rotating freely |
| CN104402137B (en) * | 2014-06-13 | 2016-03-30 | 华侨大学 | Upflowing coagulation cloth filter device and method |
| CN112028241A (en) * | 2020-07-20 | 2020-12-04 | 江苏大学 | Novel sewage purification groove device |
| CN114409207A (en) * | 2022-03-29 | 2022-04-29 | 汕头市万腾纸业有限公司 | Printing ink effluent disposal system |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1212983C (en) * | 2002-08-06 | 2005-08-03 | 巢守东 | Technique for recycling sewage generated by making beer |
| CN1199890C (en) * | 2002-12-24 | 2005-05-04 | 中国科学院生态环境研究中心 | Domestic sewage treating method and use |
| CN1208261C (en) * | 2002-12-26 | 2005-06-29 | 上海理工大学 | Normal water SBR treating method and device for kitchen sewage |
| CN101172744B (en) * | 2007-11-20 | 2011-06-15 | 中国科学院南京地理与湖泊研究所 | Process method and device for dimethyl ether production wastewater recycled for cooling water |
-
2009
- 2009-02-04 CN CN 200910077947 patent/CN101475293B/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104402137B (en) * | 2014-06-13 | 2016-03-30 | 华侨大学 | Upflowing coagulation cloth filter device and method |
| CN104860473A (en) * | 2015-05-08 | 2015-08-26 | 昆明理工大学 | Urban wastewater treatment system |
| CN104860473B (en) * | 2015-05-08 | 2016-09-21 | 昆明理工大学 | A kind of town sewage treatment system |
| CN105152498A (en) * | 2015-10-26 | 2015-12-16 | 河海大学 | Fish-gill-type oxygen-carrying purification system capable of rotating freely |
| CN112028241A (en) * | 2020-07-20 | 2020-12-04 | 江苏大学 | Novel sewage purification groove device |
| CN114409207A (en) * | 2022-03-29 | 2022-04-29 | 汕头市万腾纸业有限公司 | Printing ink effluent disposal system |
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Effective date of registration: 20160129 Address after: 065001 Hebei province Langfang Development Zone Huaxiang new Austrian Science Park Building No. 118 B Patentee after: Environmental Protection Technology Co., Ltd. Address before: 065001 Hebei city in Langfang Province Economic Development Zone East Huaxiang Xinyuan science and Technology Park B District Patentee before: ENN SCIENCE & TECHNOLOGY DEVELOPMENT Co.,Ltd. |