CN203960003U - Process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water - Google Patents
Process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water Download PDFInfo
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- CN203960003U CN203960003U CN201420324546.8U CN201420324546U CN203960003U CN 203960003 U CN203960003 U CN 203960003U CN 201420324546 U CN201420324546 U CN 201420324546U CN 203960003 U CN203960003 U CN 203960003U
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Abstract
The utility model discloses the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water, it is characterized in that: the hydrolysis acidification pool (1), up-flow anaerobic sludge blanket (UASB) reactor (2), first carrier fluidized bed (3), activated sludge tank (4), Second support fluidized-bed (5), settling tank (6), Fenton (Fenton) reaction tank (7), ozone oxidation pond (8), the rear biochemistry pool (9) that comprise mutual configuration.It is COD, the ammonia nitrogen in the art breading waste water of core that the utility model adopts " acidication+UASB+ is carrier fluidized bed+biochemistry of Fenton oxidation+catalytic ozonation+afterwards ", efficient biochemical system and advanced catalytic oxidation technique are mutually combined, organic pollution materials in fast degradation sewage, make inlet COD concentration up to 20000mg/L, ammonia nitrogen during up to 600mg/L, final outflow water COD, ammonia nitrogen reach respectively 120mg/L, below 15mg/L, reach and surpass emission standard, being specially adapted to the processing of high gravity fermentation class pharmacy waste water.
Description
Technical field
The utility model relates to the treatment process system of trade effluent, relates in particular to the process system for the treatment of high gravity fermentation class, chemosynthesis class and pharmacy waste water.
Background technology
According to incompletely statistics, have at home at present Si Qian many enterprises unit to be engaged in medicine and produce and research work, produce kind more than 10,000, the medication of nearly 1,000,000 tons of (t) starting material of annual production, the development of relevant new drug is also in carrying out endlessly.Although pharmaceutical industry total output value only accounts for 1.6% left and right in the whole nation, its wastewater discharge has accounted for more than 2%.According to statistics, pharmaceutical industry waste water annual emissions reaches 2.5 * 10
8t, chemical oxygen demand (COD) is about 1.51 * 10
5t, annual processing rate is less than 30%.
The high concentrated organic wastewater producing in pharmacy procedure, mainly comprise the washing water of production of antibiotics waste water, synthetic drugs factory effluent and all kinds of preparation production processes and flushing waste water etc., wherein, fermentation class, the pharmacy of chemosynthesis class are that Focal point and difficult point is controlled in the pollution of pharmaceutical industry, in pharmaceutical industry production process, because of starting material complicated, cause waste water complicated component.Pharmacy waste water feature is as follows: 1. the pharmacy waste water water yield and water quality change with the variation of production technique, mostly are intermittently discharged, causes draining water quality inhomogeneous, and water quality and quantity changes greatly.2. contained organic components complicated and changeable, containing heterocyclic and hard-degraded substance is many, strong to microbe-inhibiting, toxicity is large, colourity is dark and saltiness is high.3. organic content is high, and COD and scope are 20000-50000mg/L conventionally, and water quality slant acidity, belongs to typical high concentrated organic wastewater.Therefore,, in the urgent need to finding the treatment process of efficient degradation pharmaceutical wastewater, realize comprehensive, the stably reaching standard discharge of enterprise's efflux wastewater.
Be still at present both at home and abroad and take processing mode that materialization is combined with biophase as main.As adopt membrane separation technique, anaerobic-aerobic combination technique, acidication+catalytic oxidation, up-flow anaerobic sludge blanket (UASB) reactor+sequencing batch active sludge (SBR), upflow sludge blanket-strainer (UBF)+cyclic activated sludge system (CASS) etc., enforcement along with < < GB21903-2008 fermentation class pharmaceutical industry pollution discharge standard > > and < < GB21904-2008 chemosynthesis class pharmaceutical industry pollution discharge standard > >, the technique that materialization is combined with biophase can not meet the demands, advanced treatment becomes necessary, this has more increased the cost that pharmacy waste water is processed, environmental requirement has become the important factor that the numerous bio-pharmaceuticals of restriction manufacturing enterprise further develops.Traditional method is at aspect Shortcomings such as processing efficiency, secondary pollution and processing costs, be difficult to realize the qualified discharge of pharmacy waste water, and due to the deficiency of the aspects such as design, operational management, there is the problems such as construction investment is large, working cost is high, technical process is complicated, purification efficiency is not high in Waste Water Treatment.
Utility model content
Technical problem to be solved in the utility model is the treatment process system of trade effluent, especially be provided for processing the process system of high gravity fermentation class, chemosynthesis class and pharmacy waste water, solve the deficiency that the purification efficiency that exists in above-mentioned prior art and processing cost exist, organic pollution materials in this treatment system energy fast degradation sewage, make final outflow water COD, ammonia nitrogen reach respectively 200mg/L, below 15mg/L, reached and surpassed emission standard, the processing of be particularly useful for fermenting the field waste water such as class, chemosynthesis class, biochemical industry pharmacy waste water.
Technical problem to be solved in the utility model is achieved through the following technical solutions:
For the treatment of the process system of high gravity fermentation class or chemosynthesis class pharmacy waste water, comprise the hydrolysis acidification pool, up-flow anaerobic sludge blanket (UASB) reactor of mutual configuration, first carrier fluidized bed, activated sludge tank, Second support fluidized-bed, settling tank, Fenton's reaction tower, ozone oxidation pond, rear biochemistry pool.Described mutual configuration refers to by water pipe and pump and interconnects.
Described hydrolysis acidification pool is provided with heating rod.
Described up-flow anaerobic sludge blanket (UASB) reactor front end is provided with line mixer and adds supplementary phosphoric and alkali;
Described up-flow anaerobic sludge blanket (UASB) inside reactor is provided with water distributor, triphase separator, some thief holes; Described thief hole arranges along height for reactor direction,
In described reactor, be provided with pneumatic diaphragm pump and carry out internal recycling.
In described first carrier fluidized bed, Second support fluidized-bed, be provided with floating stuffing.Described floating stuffing main material is high density polyethylene(HDPE) (HDPE), nominal diameter: 25 ± 2mm, and nominal length: 10 ± 1mm, carrier filler tap density is: 98 (± 1) kg/m
3.
Described the first carrier fluidized bed and floating stuffing filling ratio Second support fluidized-bed is 20-60%.
Described hydrolysis acidification pool residence time 5-20h; Up-flow anaerobic sludge blanket (UASB) reactor residence time 20-100h; 1# is carrier fluidized bed, activated sludge tank, the carrier fluidized bed residence time 20-50h of 2#; Settling tank residence time 2-8h; Fenton (Fenton) reaction tower residence time 2-6h; Ozone oxidation pond residence time 1-5h, rear biochemistry pool residence time 6-20h.
Described first carrier fluidized bed, activated sludge tank, Second support fluidized-bed bottom are provided with aerating apparatus; Described aerating apparatus is communicated with aerator.
Described settling tank is by air-lift device and the first carrier fluidized bed connection.Described Fenton (Fenton) reaction tank is connected by lift pump with ozone oxidation pond;
Described ozone oxidation pond is that some ponds body is in series or in parallel with each other.Described ozone oxidation pond is connected with ozonizer.Described ozone oxidation pond is connected with tail gas breaking plant;
In described ozone oxidation pond, being filled with volume ratio is the carrying transition metal ionic catalyst of 20%-100%, carrying transition metal ionic catalyst is ozone oxidation catalyst, can be one or more compositions that are mixed in gac, silica gel, haydite, zeolite, molecular sieve, aluminium sesquioxide, one or more of load Fe, Cu, Mn, Co, Pd, Ni, Mn be active ingredient; Described floating stuffing main material is high density polyethylene(HDPE).
The utility model adopts technique scheme, and the feature and the advantage that compared with prior art had are:
1. " acidication+UASB+ is carrier fluidized bed+biochemistry of Fenton oxidation+catalytic ozonation+afterwards " is the COD in the process integration device processes pharmacy waste water of core to this combined process system based on adopting, ammonia nitrogen, make inlet COD concentration up to 20000mg/L, ammonia nitrogen is during up to 600mg/L, final outflow water COD, ammonia nitrogen reaches respectively 100mg/L, below 15mg/L, reach the emission standard of < < GB21903-2008 fermentation class pharmaceutical industry pollution discharge standard > > and < < GB21904-2008 chemosynthesis class pharmaceutical industry pollution discharge standard > > regulation, drug cost after technical process is processed is about 10 yuan, water per ton.
2. the organic pollution materials in this combined process system energy fast degradation sewage, make final outflow water COD, ammonia nitrogen reach respectively 200mg/L, below 15mg/L, reached the emission standard of GB8978-1996 < < integrated wastewater discharge standard > > regulation, the processing of be especially applied to ferment the field waste water such as class, chemosynthesis class, biochemical industry pharmacy waste water.
3. the utility model COD clearance is high, under the effect of carrying transition metal ionic catalyst, produces comprehensive and fierce oxidizing reaction, to remove or the COD composition of the high difficult degradation of decomposition and inversion, and then reaches the object that removes COD.
4. carrier fluidized bed system adopts unique floating stuffing, is beneficial to the microorganism growth of degraded hardly degraded organic substance, and biological flora is abundant, and effluent quality is good.
5. the utility model floor space is little, and the completion time of project is short, and running cost is low, and processing costs economizes, and has obvious economic and social benefit.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the utility model is described further.
Fig. 1 is the utility model process flow sheet
Fig. 2 is the utility model process system structural representation
Fig. 3-1 is the utility model floating stuffing structural representation
Fig. 3-2 are the side-view of Fig. 3-1
In figure: 1-hydrolysis acidification pool, 2-up-flow anaerobic sludge blanket (UASB) reactor, 3-first is carrier fluidized bed, 4-activated sludge tank, 5-Second support fluidized-bed, 6-settling tank, 7-Fenton (Fenton) reaction tank, 8-ozone oxidation pond, biochemistry pool after 9-, 10-heating rod, 11-line mixer, 12-water distributor, 13-triphase separator, the some thief holes of 14-, 15-pneumatic diaphragm pump, 16-aerating apparatus, 17-aerator, 18-air-lift device, 19-floating stuffing, 20-external toroidal ring, ring in 21-, 22-is gusset radially, the little fin of 23-, 24-radial radiation fin, 25-connects gusset, 26-chamber, 27-lift pump, 28-ozonizer, 29-tail gas breaking plant.
Embodiment
As Fig. 1, Fig. 2, described in Fig. 3 for the treatment of the process system of high gravity fermentation class or chemosynthesis class pharmacy waste water: comprise the hydrolysis acidification pool 1 mutually configuring by water pipe and pump, up-flow anaerobic sludge blanket (UASB) reactor 2, first carrier fluidized bed 3, activated sludge tank 4, Second support fluidized-bed 5, settling tank 6, Fenton (Fenton) reaction tank 7, ozone oxidation pond 8, rear biochemistry pool 9, heating rod 10, line mixer 11, water distributor 12, triphase separator 13, some thief holes 14, pneumatic diaphragm pump 15, aerating apparatus 16, aerator 17, air-lift device 18, floating stuffing 19, external toroidal ring 20, interior ring 21, radially gusset 22, finlet sheet 23, radial radiation fin 24, connect gusset 25, chamber 26, lift pump 27, ozonizer 28, tail gas breaking plant 29.
The effect of native system concrete technology process step and each section of equipment is as follows:
(1) waste water, as pharmacy waste water, adopts volume pump to pump into hydrolysis acidification pool 1, and described hydrolysis acidification pool is provided with heating rod 10, makes inflow temperature be maintained at about 30 ℃, and waste water is first processed.Water delivery hydrolysis acidification pool plays and regulates water water quality and the water yield, the effect of minimizing to the impact of subsequent disposal unit, in waste water, organism is tentatively degraded at hydrolysis acidification pool, and larger molecular organics resolves into small organic molecule, can improve follow-up biochemical treatment efficiency;
(2) 1 water outlet of said hydrolyzed acidification pool enters up-flow anaerobic sludge blanket (UASB) reactor 2, up-flow anaerobic sludge blanket (UASB) its feature of reactor and advantage are mainly reflected in formation granule sludge, sludge concentration in reactor is increased substantially, and therefore hydraulic detention time shortens greatly; Meanwhile, in up-flow anaerobic sludge blanket (UASB) reactor, triphase separator 13 is set, saved settling tank, thereby structure is also simpler.
If lack phosphoric in waste water, line mixer throwing 11 can be set before UASB reactor 2 and add supplementary phosphoric; Simultaneously can add as required alkali in good time, as NaOH, guarantee that described up-flow anaerobic sludge blanket (UASB) reactor 2, in most suitable pH value, is convenient to maintain anaerobic methanogens in reactor and has stable reaction environment.
On up-flow anaerobic sludge blanket in native system (UASB) reactor 2, be provided with some thief holes 14, along height for reactor direction, arrange, be convenient to observe mud situation and sampling.For strengthening contacting of mud and waste water, described reactor arranges a pneumatic diaphragm pump 15 and carries out internal recycling, has effectively accelerated speed of reaction.Through above-mentioned processing, in described UASB reactor, the most COD of waste water is removed.
(3) water outlet of above-mentioned up-flow anaerobic sludge blanket (UASB) reactor enters first carrier fluidized bed 3, activated sludge tank 5 successively, Second support fluidized-bed carries out respectively the removal of organism and ammonia nitrogen.The described carrier fluidized bed floating stuffing 19 that adopted, under the disturbance of blast aerator 16, in reaction tank, with current, float, make carrier fluidized bed more traditional biochemical process equipment there is higher sludge concentration, more uniform fluidized, the microorganism of apposition growth can reach very high biomass, biological concentration can reach 2～4 times of traditional suspension growth activated sludge process in reaction tank, can reach 8～12g/L, therefore degradation efficiency also significantly improves, thereby obtains better decontamination effect improving.This process section has adopted the carrier fluidized bed abundant balance of two-stage and has processed the contradiction between load and construction investment, has reduced suspended biological filler dosage.
(4) above-mentioned carrier fluidized bed water outlet enters settling tank 6, carries out mud-water separation, and settling tank adopts vertical sedimentation basin, in vertical sedimentation basin, sewage is vertically to flow from the top down, and suspended substance sedimentation enters in the heavy bucket of pond base cone shape, and primary water goes out along peripheral overflow weir flow from pond surrounding.The advantage of vertical sedimentation basin is that floor space is little, and spoil disposal is easy.Part mud is by air-lift device, is back to front end first carrier fluidized bed 3, maintains system inner suspension sludge concentration.
(5) pharmacy waste water is carrier fluidized bed 3 through first, and activated sludge tank 4, after Second support fluidized-bed biochemical 5 is processed, most of organism is processed, remaining is hardly degraded organic substance, has been difficult to further degrade by biochemical treatment, must carry out advanced treatment.
The water outlet of described settling tank adds a certain amount of sulfuric acid, hydrogen peroxide, ferrous sulfate is first carries out oxidizing reaction processing in Fenton (Fenton) reaction tank.Fenton oxidation style can produce a large amount of hydroxy radical qiaos (OH) in reaction, and it is a kind of very active and non-selective species, and its oxidizing potential is 2.8V, and oxidation capacity is very strong, can cause most of organic redox reaction in the aqueous solution.But Fenton method need to consume a large amount of bronsted lowry acids and bases bronsted lowry class materials separately, can produce a large amount of mud.Therefore in order to take into account advanced treatment effect and working cost, this process system has reduced the reagent dosage of Fenton oxide treatment, suitably improves water outlet COD value, its water outlet is incorporated into ozone oxidation pond 8 and carries out catalytic ozonation processing.Catalytic ozonation technique is to process at present the generally acknowledged modern technique of high density, organic wastewater with difficult degradation thereby, the feature of this technology is that ozone oxidation agent is under the effect of the carrying transition metal ionic catalyst of newly developing, free radical in effective generation and increase reaction system, thereby produce comprehensive and fierce oxidizing reaction, to remove or the COD composition of the high difficult degradation of decomposition and inversion.Catalytic ozonation reaction need not be carried out under high temperature, high pressure, under usual conditions, can reach reaction requirement, obtains very high oxide treatment efficiency.
(6) water outlet after above-mentioned oxidation enters into rear biochemistry pool and carries out aerobic treatment.Waste water is after peroxidation, and wastewater biodegradability is improved, and adopts the processing of aerobic biochemical to waste water, and wastewater through organic matter is further removed, and required expense is also very low simultaneously.
This combined process system trial run example one
Guangdong drugmaker is domestic important yeast production base.In the production process of yeast, take waste molasses as raw material, after yeast utilizes, discharge the organic waste water of a large amount of high densitys, high chroma, waste water is comprised of yeast acidizing fluid flash trapping stage waste water, the second-order separation waste water, three grades of separated waste water, various flushing waste waters etc., for satisfied environmental requirement needs are processed this strand of sewage.
Experiment condition is as follows:
This experiment pharmacy waste water treatment capacity is 20L/h, and COD is about 20000mg/L, pH value between 4～5, ammonia nitrogen 100-600mg/L.1 residence time of hydrolysis acidification pool 10h; Up-flow anaerobic sludge blanket (UASB) 2 residence time of reactor 70h, circular flow 180～300L/h, phosphoric acid dosage 180mg/L; The first carrier fluidized bed 3 residence time 45h, 4 residence time of activated sludge tank 45h, 4 residence time of Second support fluidized-bed 34h; 6 residence time of settling tank 4h, sludge reflux amount 20～80L/h; Fenton (Fenton) 7 residence time of reaction tank 4h, sulfuric acid, ferrous sulfate dosage are 2000mg/L, hydrogen peroxide dosage 1200mg/L; 8 residence time of ozone oxidation pond 1h, ozone dosage 200mg/L; Rear 9 residence time of biochemistry pool 10h.Get respectively many group experiments and carry out each unit water outlet COD, ammonia nitrogen determination.Each unit water outlet COD data are as following table 1, and ammonia nitrogen water outlet can reach below 15mg/L, and through calculating, reagent consumption expense is about 10 yuan of water per ton.
Table 1: each unit water outlet COD data unit mg/L
Experiment shows: for the water quality characteristics of pharmacy waste water, adopting native system " acidication+UASB+ is carrier fluidized bed+biochemistry of Fenton oxidation+catalytic ozonation+afterwards " is the process integration Pharmaceutical Wastewater Treatment of core, through the test of 5L/h high gravity fermentation class pharmacy waste water Continuous Flow lab scale, make inlet COD concentration up to 20000mg/L, ammonia nitrogen is during up to 600mg/L, final outflow water COD, ammonia nitrogen reaches respectively 100mg/L, below 15mg/L, reach the emission standard of < < GB21903-2008 fermentation class pharmaceutical industry pollution discharge standard > > and < < GB21904-2008 chemosynthesis class pharmaceutical industry pollution discharge standard > > regulation, technical process reagent consumption expense is about 10 yuan of water per ton.This technological advantage is that efficient biochemical system and advanced catalytic oxidation technique are mutually combined, and seeks a kind of combined process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water significant.
Above-described embodiment, just the selected embodiment of the utility model is a kind of, and the not restriction to embodiment.For a person skilled in the art, can also make on the basis of the above description other multi-form change.The apparent variation of amplifying out thus and replacement all should be included in protection domain of the present utility model.
Claims (9)
1. for the treatment of the process system of high gravity fermentation class or chemosynthesis class pharmacy waste water, it is characterized in that: comprise the hydrolysis acidification pool (1), upflow anaerobic sludge blanket reactor (2), first carrier fluidized bed (3), activated sludge tank (4), Second support fluidized-bed (5), settling tank (6), Fenton's reaction pond (7), ozone oxidation pond (8), the rear biochemistry pool (9) that are linked in sequence successively.
2. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described hydrolysis acidification pool (1) is provided with heating rod (10).
3. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, it is characterized in that: described upflow anaerobic sludge blanket reactor (2) front end is provided with line mixer (11), inside is provided with water distributor (12), triphase separator (13), some thief holes (14); In described upflow anaerobic sludge blanket reactor (2), be provided with pneumatic diaphragm pump (15).
4. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described first carrier fluidized bed (3), activated sludge tank (4), Second support fluidized-bed (5) bottom are provided with aerating apparatus (16); Described aerating apparatus (16) is communicated with aerator (17).
5. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described settling tank (6) is communicated with by air-lift device (18) carrier fluidized bed with first (3).
6. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: in described first carrier fluidized bed (3), Second support fluidized-bed (5), be provided with floating stuffing (19); Described floating stuffing (19) comprises external toroidal ring (20), interior ring (21), radially gusset (22), little fin (23), radial radiation fin (24); Described external toroidal ring (20) is connected by two described radially gussets (21) that intersect vertically with interior ring (21); Between described external toroidal ring and interior ring, be provided with and connect gusset (25); Between described external toroidal ring and interior ring, form a plurality of chambers (26); Described radial radiation fin (24) is disposed on the outer surface of external toroidal ring (20); Described little fin (23) is disposed on the outer surface of interior ring (21).
7. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described Fenton's reaction pond (7) is connected by lift pump (27) with ozone oxidation pond (8).
8. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described ozone oxidation pond (8) is that some ponds body is in series or in parallel with each other; Described ozone oxidation pond (8) is connected with ozonizer (28); Described ozone oxidation pond (8) is connected with tail gas breaking plant (29).
9. the process system for the treatment of high gravity fermentation class or chemosynthesis class pharmacy waste water according to claim 1, is characterized in that: described mutual configuration refers to by water pipe and pump and interconnects.
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| CN104710077A (en) * | 2015-03-06 | 2015-06-17 | 天津市联合环保工程设计有限公司 | Treatment system and treatment method of synthetic rubber wastewater |
| CN104710077B (en) * | 2015-03-06 | 2017-03-01 | 天津市联合环保工程设计有限公司 | The processing system of synthetic rubber waste water and its processing method |
| 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 |
| CN105174640A (en) * | 2015-10-10 | 2015-12-23 | 浙江巨能环境工程设备有限公司 | Biochemical treatment process for paint-producing wastewater |
| CN106315977A (en) * | 2016-09-09 | 2017-01-11 | 华纺股份有限公司 | Printing and dyeing wastewater treatment technique |
| CN106315977B (en) * | 2016-09-09 | 2019-05-17 | 华纺股份有限公司 | A kind of printing-dyeing waste water treatment process |
| CN110240365A (en) * | 2019-07-18 | 2019-09-17 | 四川恒泰环境技术有限责任公司 | A kind of coal chemical industry high concentration wastewater treatment system and its method |
| CN113562903A (en) * | 2021-08-16 | 2021-10-29 | 天津海派特环保科技有限公司 | Multi-cycle oxidation device and treatment process for high-salt degradation-resistant COD sewage treatment |
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