CN103043789A - Anaerobic reactor and treatment method of cotton pulp production waste water - Google Patents
Anaerobic reactor and treatment method of cotton pulp production waste water Download PDFInfo
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Abstract
The invention provides an anaerobic reactor and a treatment method of cotton pulp production waste water. The cotton pulp production waste water is sequentially subjected to hydrolytic treatment, anaerobic treatment, aerobic treatment and coagulation treatment; the anaerobic reactor comprises a housing and a gas-liquid separator; the housing is sequentially provided with a first reaction area, a second reaction area and a sediment area from the bottom up; a water inlet pipe is arranged at the lower part of the first reaction area; a first gas-collecting hood is arranged at the upper part of the first reaction area, and communicated with the gas-liquid separator by a methane lift pipe; a biological filler is arranged at the upper part of the second reaction area; a second gas-collecting hood is arranged above the biological filler, and communicated with the gas-liquid separator by a gas-collecting pipe; the sediment area is provided with a water outlet pipe; the gas-liquid separator is communicated with the first reaction area by a return pipe; the concentration of sludge subjected to the anaerobic treatment is 5g/L-10g/L; and the hydraulic retention time is 16h-22h. The treatment method can increase a removal rate of the anaerobic treatment.
Description
Technical field
The present invention relates to technical field of waste water processing, particularly the treatment process of a kind of anaerobic reactor and cotton pulp factory effluent.
Background technology
Pulping and papermaking industry is traditional water rich and influential family, also is one of important source of pollution that cause the water pollution.At present, China's paper-making industrial waste water quantity discharged and the COD quantity discharged first place that all occupies China's all types of industries quantity discharged.Along with expanding economy, enterprise faces the problems such as shortage of water resources and scarcity of raw material day by day, and on the other hand, water pollutes also more and more serious.Therefore, how effectively processing the not matter of utmost importance of China's industrial pollution caused by paper manufacturing control still of paper-making effluent, also is the matter of utmost importance that national trade effluent carries out processing up to standard, and significant to enterprise development.
Cotton pulp production is the industry of traditional highly energy-consuming and high pollution, and the cotton pulp factory effluent belongs to a kind of of paper-making effluent, and its processing problem is the insoluble problem of national cotton pulp industry always.Pollutant component in the cotton pulp factory effluent mainly contains: the suspended substances such as (1) Mierocrystalline cellulose and Mierocrystalline cellulose fines; (2) organism of the readily biodegradable such as hemicellulose and oligose; (3) organism of difficult for biological degradation, such as xylogen, it is benzyl ring propane polymkeric substance, molecular weight between 5000 ~ 50000, close structure, stable performance.For the processing of cotton pulp factory effluent, generally mainly contain alkali recycling method, acid-precipitation method, Coagulation Method, membrane separation process and biological process etc.Present domestic most cotton pulp manufacturing enterprise substantially all adopts hydrolysis-aerobic-coagulation process that waste water is carried out tertiary treatment, minority enterprise adopts hydrolysis, anaerobic-aerobic-coagulation process, wherein, anaerobism operation during the first step is processed generally realizes by common Anaerobic cultural methods, such as anaerobic pond method, anaerobic filter bed method, anaerobism fluidized bed method, anaerobic baffled reactor method (ABR), sequencing batch reactor method (SBR), anaerobic pond method and upflow anaerobic sludge blanket process method (UASB) etc.
Because the biodegradability of cotton pulp factory effluent is lower, the BOD/COD value generally only has about 0.2, so that the anaerobism clearance (COD clearance) that the first step is processed in the prior art generally only has an appointment 30%, processing efficiency is low, therefore directly increased the pressure that the second stage, the third stage are processed, finally causing the third stage to process used flocculation agent consumption increases, and makes the comprehensive treating process cost high.
Summary of the invention
In order to solve above technical problem, the invention provides the treatment process of a kind of anaerobic reactor and cotton pulp factory effluent, the anaerobism clearance of anaerobic treatment is higher in the method, so that cost is lower, is suitable for promoting.
The invention provides a kind of anaerobic reactor, comprise housing and gas-liquid separator;
Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe;
Described gas-liquid separator communicates with described the first reaction zone by return line.
Preferably, be provided with annular rising pipe between described the second gas skirt and the described biologic packing material;
The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
The invention provides a kind for the treatment of process of cotton pulp factory effluent, comprising:
With cotton pulp factory effluent be hydrolyzed successively processing, anaerobic treatment, aerobic treatment and coagulating treatment;
The anaerobic reactor of described anaerobic treatment comprises housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe; Described gas-liquid separator communicates with described the first reaction zone by return line;
The sludge concentration of described anaerobic treatment is 5g/L ~ 10g/L, and hydraulic detention time is 16 hours ~ 22 hours.
Preferably, be provided with annular rising pipe between described the second gas skirt and the described biologic packing material;
The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
Preferably, the temperature of described anaerobic treatment is 25 ℃ ~ 35 ℃, and the pH value is 6 ~ 8.
Preferably, be hydrolyzed before the processing, the cotton pulp factory effluent is filtered, the pH value of the waste water after then will filtering is adjusted to 6 ~ 9.
Preferably, the temperature of described hydrolysis treatment is 25 ℃ ~ 35 ℃, and the pH value is 6 ~ 9, and sludge concentration is 3g/L ~ 6g/L, and hydraulic detention time is 6 hours ~ 10 hours.
Preferably, the temperature of described aerobic treatment is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and sludge concentration is 3g/L ~ 6g/L, and hydraulic detention time is 20 hours ~ 24 hours, and dissolved oxygen is 1.0mg/L ~ 3.0mg/L.
Preferably, after aerobic treatment, before the coagulating treatment, also comprise precipitation process, the temperature of described precipitation process is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and hydraulic detention time is 8 hours ~ 12 hours.
Preferably, the temperature of described coagulating treatment is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and hydraulic detention time is 8 hours ~ 12 hours, and dosage of PAC is 3 ‰ ~ 5 ‰.
Compared with prior art, the treatment process of cotton pulp factory effluent provided by the invention comprises: with the cotton pulp factory effluent be hydrolyzed successively, anaerobism, aerobic and coagulating treatment; The anaerobic reactor of described anaerobic treatment comprises housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe; Described gas-liquid separator communicates with described the first reaction zone by return line; The sludge concentration of described anaerobic treatment is 5g/L ~ 10g/L, and hydraulic detention time is 16 hours ~ 22 hours.The present invention uses and is fit to the anaerobic reactor that the cotton pulp factory effluent carries out degree of depth anaerobic treatment, and by controlling the processing condition of anaerobic treatment, biosolids concentration is greatly improved, but the material Partial digestion to hard degradation, and can improve the biodegradability of waste water, and make the mud total amount maintain higher level, prolonged the biological residence time, DeR is stable carries out the anaerobism clearance of Effective Raise anaerobic treatment stage thereby make.Practice shows that the anaerobism clearance for the treatment of process provided by the invention can maintain more than 60%.The efficient of anaerobic treatment of the present invention is higher, and the load that enters the materialization flocculation process is reduced near 50%, reduces the expense of flocculation medicament, and the biogas amount of generation is increased, and save energy reduces cost.
Description of drawings
Fig. 1 is the structural representation of the used anaerobic reactor of one embodiment of the invention.
Embodiment
In order further to understand the present invention, below in conjunction with embodiment the preferred embodiment of the invention is described, but should be appreciated that these describe just as further specifying the features and advantages of the present invention, rather than to the restriction of claim of the present invention.
The invention provides a kind of anaerobic reactor, comprise housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe;
Described gas-liquid separator communicates with described the first reaction zone by return line.
The used anaerobic reactor of the present invention is a kind of improved high efficiency anaerobic reactor, and it possesses a lot of good characteristics, can realize the degree of depth anaerobic treatment to the cotton pulp factory effluent.
During described anaerobic reactor work, waste water can enter the first reaction zone by water inlet pipe, mixes with granule sludge, most of organism is degraded at this, produces a large amount of biogas, and biogas is collected by the first gas skirt, that is to say that first step triphase separator is mainly for separating of the natural pond G﹠W.Because gas production rate is large and the liquid phase upflow velocity is very fast, biogas, waste water can not finely separate with mud, formed gas, Gu, the liquid mixed stream, again owing to the pressure of the pressure in the triphase separator less than reaction zone, mixing liquid enters in the triphase separator under the effect of carrying secretly of biogas, breaking away from mixed solution at this most of biogas effluxes, it is large that the density of mixed stream becomes, under action of gravity, be back to the bottom of the first reaction zone by return line, waste water with the first reaction zone, granule sludge mixes, thereby realized the circulation of fluid at inside reactor, the liquid phase upflow velocity of the first reaction zone is increased greatly.
Described the first reaction zone has the organic ability of very large removal, subsequently, enters second reaction zone through the liquid phase of the first reaction zone, proceeds biological respinse, removes the residual organic substances in the waste water, and the biogas of generation is collected by the second gas skirt.In addition, the breeze way between the first reaction zone and the settling region is also served as in this zone, to guaranteeing that precipitating rear effluent quality plays an important role.That is to say that second stage triphase separator is mainly for separating of mud and water.
In the present invention, described second reaction zone top is provided with biologic packing material, its height can design, like this unloading phase of the anaerobic reactor sludge acclimatization, the surface of filler can form the microbial population with the growth of microbial film form, in the space of filler, then held back the anaerobion of a large amount of suspension growths, after being degraded through two reaction zones, continues waste water upwards to flow, during through microbial film, organism in the waste water is trapped, adsorbs and decomposes, and a small amount of floc sludge also can be trapped, adsorb simultaneously.
The present invention has increased biologic packing material in internal-circulation anaerobic reactor inside, mud method and the membrane process craft of anaerobic treatment are organically combined, make anaerobic reactor not only possess all advantages of inner circulation reactor, and many advantages of anaerobic biofilter have been increased, the advantage that is described anaerobic reactor comprises: (1) biosolids concentration improves, and organic loading can continue to improve; (2) sludge retention time (SRT) is long, can shorten hydraulic detention time (HRT), a large amount of recirculated water and water inlet fully mix, and the objectionable impurities in the former water is fully diluted, greatly reduce poisonous substance to the impact of anaerobic digestion process, the anti impulsion load ability strengthens; (3) reduce start time, restarting also after out of service is easier to; (4) reduced to greatest extent sludge loss, made the mud total amount maintain higher level, prolonged the biological residence time, DeR is stable carries out Effective Raise anaerobism clearance thereby make; (5) operation stability improves, and operational management is convenient; Etc..
At last, the waste water of process second reaction zone enters the settling region, and the waste water after the precipitation is discharged from rising pipe, and the biogas that produces in the whole treating processes is discharged via gas-liquid separator.
As preferably, the present invention is provided with annular rising pipe between described the second gas skirt and described biologic packing material; The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
The present invention increases annular rising pipe between filler and second stage triphase separator, after compiling, passes through waste water recycle pump, enter the first reaction zone from the water inlet pipe of reactor bottom, can improve contacting and reaction between matrix and the microorganism in the reactor, can process at a lower temperature the organic waste water of low concentration, this has just possessed some advantages of expanded bed reactor (EGSB).
In one embodiment of the invention, inherent each the gas skirt place of housing all is symmetrically arranged with sealing gland, makes gas skirt can collect better gas.
Fig. 1 is the structural representation of the used anaerobic reactor of one embodiment of the invention, and its height is 22 meters, and diameter is 8 meters;
In Fig. 1,1 is housing, and 11 is water inlet pipe, introduces the cotton pulp factory effluent; 12 is the first gas skirt, highly is being 10 meters; 13 is the second gas skirt, highly is being 20 meters; 14 is rising pipe, the waste water after the discharge anaerobic treatment; 15 is the first reaction zone, between the bottom and the first gas skirt 12 of housing 1; 16 is second reaction zone, between the first gas skirt 12 and the second gas skirt 13; 17 is the settling region, between the top of the second gas skirt 13 and housing 1; 18 is biologic packing material, at 13 times 1 meter to 5 meters of the second gas skirt; 19 is sealing gland;
2 is gas-liquid separator, discharges biogas; Gas-liquid separator 2 is communicated with the second gas skirt 12 by effuser 3, is communicated with the first gas skirt 12 by biogas-lift pipe 4, communicates with the first reaction zone 15 by return line 5;
6 is recycle pump, and its entrance is communicated with annular rising pipe (not marking in Fig. 1) between the second gas skirt 13 and the biologic packing material 18, and outlet is communicated with water inlet pipe 11.
The invention provides a kind for the treatment of process of cotton pulp factory effluent, comprising:
With the cotton pulp factory effluent be hydrolyzed successively, anaerobism, aerobic and coagulating treatment;
The anaerobic reactor of described anaerobic treatment comprises housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe; Described gas-liquid separator communicates with described the first reaction zone by return line;
The sludge concentration of described anaerobic treatment is 5g/L ~ 10g/L, and hydraulic detention time is 16 hours ~ 22 hours.
The present invention's processing that at first the cotton pulp factory effluent is hydrolyzed makes the organism macromole be converted into small molecules, in order to carry out subsequent handling.
Be hydrolyzed before the processing, the present invention preferably filters the cotton pulp factory effluent, and the pH value of the waste water after then will filtering is adjusted to 6 ~ 9.
The cotton pulp factory effluent filters through filter screen, removes fiber fines and recycled fiber, the waste water after obtaining filtering.Describedly be filtered into technique means well known to those skilled in the art, wherein, it is 30m that described filter screen is preferably the wire side area
2, the order number is the oblique nets of 100 purposes.
Behind the waste water after obtaining filtering, the present invention preferably carries out the pH value to it and regulates, and adds hydrochloric acid such as the waste water after filter, and ensures that water outlet pH value is 6 ~ 9, obtains the middle wastewater after the acid adjustment, is beneficial to the processing that is hydrolyzed.
After obtaining the middle wastewater after the acid adjustment, be introduced into the hydrolysis acidification pool processing that is hydrolyzed.In one embodiment of the invention, the volume of described hydrolysis acidification pool is preferably 3000m
3The actual conditions of described hydrolysis treatment is preferably: temperature is 25 ℃ ~ 35 ℃, is preferably 28 ℃ ~ 32 ℃; The pH value is 6 ~ 9, is preferably 7 ~ 9; Sludge concentration is 3g/L ~ 6g/L, is preferably 3g/L ~ 4g/L; Hydraulic detention time is 6 hours ~ 10 hours, is preferably 8 hours ~ 9 hours.The hydrolysis treatment of the embodiment of the invention can be converted into small molecules with larger molecular organics in the cotton pulp factory effluent, improves wastewater biodegradability, and removes the COD in the waste water.
After hydrolysis treatment is finished, waste water after the present invention will be hydrolyzed is squeezed into the anaerobic treatment device with pump and is carried out anaerobic treatment, some organism that utilize anaerobion can not degrade to aerobic microbiological are degraded or Partial digestion, the biodegradability of cotton pulp factory effluent is further improved, thereby improve the treatment effect of follow-up aerobic treatment, and then can directly reduce third stage materialization processing costs, reduce sewage comprehensive treating process expense.
The used anaerobic reactor of the present invention is a kind of improved high efficiency anaerobic reactor, and it possesses a lot of good characteristics, can realize the degree of depth anaerobic treatment to the cotton pulp factory effluent.The anaerobic reactor of described anaerobic treatment comprises housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe; Described gas-liquid separator communicates with described the first reaction zone by return line;
Waste water after the hydrolysis enters the first reaction zone by water inlet pipe, mixes with granule sludge, and most of organism is degraded at this, produces a large amount of biogas, and biogas is collected by the first gas skirt, that is to say, first step triphase separator is mainly for separating of the natural pond G﹠W.Because gas production rate is large and the liquid phase upflow velocity is very fast, biogas, waste water can not finely separate with mud, formed gas, Gu, the liquid mixed stream, again owing to the pressure of the pressure in the triphase separator less than reaction zone, mixing liquid enters in the triphase separator under the effect of carrying secretly of biogas, breaking away from mixed solution at this most of biogas effluxes, it is large that the density of mixed stream becomes, under action of gravity, be back to the bottom of the first reaction zone by return line, waste water with the first reaction zone, granule sludge mixes, thereby realized the circulation of fluid at inside reactor, the liquid phase upflow velocity of the first reaction zone is increased greatly.
Described the first reaction zone has the organic ability of very large removal, subsequently, enters second reaction zone through the liquid phase of the first reaction zone, proceeds biological respinse, removes the residual organic substances in the waste water, and the biogas of generation is collected by the second gas skirt.In addition, the breeze way between the first reaction zone and the settling region is also served as in this zone, to guaranteeing that precipitating rear effluent quality plays an important role.That is to say that second stage triphase separator is mainly for separating of mud and water.
In the present invention, the top of described second reaction zone is provided with biologic packing material, its height can design, like this unloading phase of the anaerobic reactor sludge acclimatization, the surface of filler can form the microbial population with the growth of microbial film form, in the space of filler, then held back the anaerobion of a large amount of suspension growths, after being degraded through two reaction zones, continues waste water upwards to flow, during through microbial film, organism in the waste water is trapped, adsorbs and decomposes, and a small amount of floc sludge also can be trapped, adsorb simultaneously.
The present invention has increased biologic packing material in internal-circulation anaerobic reactor inside, mud method and the membrane process craft of anaerobic treatment are organically combined, make anaerobic reactor not only possess all advantages of inner circulation reactor, and many advantages of anaerobic biofilter have been increased, the advantage that is described anaerobic reactor comprises: (1) biosolids concentration improves, and organic loading can continue to improve; (2) sludge retention time (SRT) is long, can shorten hydraulic detention time (HRT), a large amount of recirculated water and water inlet fully mix, and the objectionable impurities in the former water is fully diluted, greatly reduce poisonous substance to the impact of anaerobic digestion process, the anti impulsion load ability strengthens; (3) reduce start time, restarting also after out of service is easier to; (4) reduced to greatest extent sludge loss, made the mud total amount maintain higher level, prolonged the biological residence time, DeR is stable carries out Effective Raise anaerobism clearance thereby make; (5) operation stability improves, and operational management is convenient; Etc..
At last, the waste water of process second reaction zone enters the settling region, and the waste water after the precipitation is discharged from rising pipe, and the biogas that produces in the whole treating processes is discharged via gas-liquid separator.
As preferably, the present invention is provided with annular rising pipe between described the second gas skirt and described biologic packing material; The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
The present invention increases annular rising pipe between filler and second stage triphase separator, after compiling, passes through waste water recycle pump, enter the first reaction zone from the water inlet pipe of reactor bottom, can improve contacting and reaction between matrix and the microorganism in the reactor, can process at a lower temperature the organic waste water of low concentration, this has just possessed some advantages of expanded bed reactor (EGSB).
In one embodiment of the invention, inherent each the gas skirt place of housing all is symmetrically arranged with sealing gland, makes gas skirt can collect better gas.
The present invention uses described anaerobic reactor, and by controlling the processing condition of anaerobic treatment, in order to the cotton pulp factory effluent is carried out degree of depth anaerobic treatment, improves anaerobic treatment efficient.In the present invention, the sludge concentration of described anaerobic treatment is 5g/L ~ 10g/L, is preferably 7g/L ~ 9g/L; The hydraulic detention time of described anaerobic treatment is 16 hours ~ 22 hours, is preferably 16 hours ~ 18 hours.
Because anaerobic treatment is comparatively responsive to temperature variation etc., in the present invention, the temperature of described anaerobic treatment is preferably 25 ℃ ~ 35 ℃, more preferably 28 ℃ ~ 32 ℃; The pH value of described anaerobic treatment is preferably 6 ~ 8, is beneficial to the cotton pulp factory effluent is carried out degree of depth anaerobic treatment.
After finishing anaerobic treatment, the present invention will introduce the aerobic aeration pond through the waste water after the anaerobic treatment, carry out aerobic treatment by aeration, make the organism in the waste water be decomposed into the innoxious substances such as carbonic acid gas and water by the aerobic microbiological oxidation, remove COD.
Described aerobic treatment is processing means well known to those skilled in the art, and in one embodiment of the invention, the volume in described aerobic aeration pond is preferably 8000m
3The actual conditions of described aerobic treatment is preferably: temperature is 20 ℃ ~ 35 ℃, is preferably 25 ℃ ~ 30 ℃; The pH value is 6 ~ 8; Sludge concentration is 3g/L ~ 6g/L; Hydraulic detention time is 20 hours ~ 24 hours, is preferably 21 hours ~ 23 hours; Dissolved oxygen is 1.0mg/L ~ 3.0mg/L, is preferably 1.0mg/L ~ 2.0mg/L; The COD removal effect of the aerobic treatment of the embodiment of the invention also promotes to some extent.
After aerobic treatment was finished, the waste water after the aerobic treatment of the present invention carried out coagulating treatment, by dosing coagulant, gravity settling, removed tiny suspended substance and colloidalmaterial in the waste water.
After aerobic treatment, before the coagulating treatment, the present invention preferably also comprises precipitation process, and the waste water after the aerobic treatment is introduced the second pond precipitating sludge.Wherein, the actual conditions of described precipitation process is: temperature is 20 ℃ ~ 35 ℃, is preferably 25 ℃ ~ 30 ℃; The pH value is 6 ~ 8; Hydraulic detention time is 8 hours ~ 12 hours, is preferably 9 hours ~ 11 hours.It is 3500m that described second pond is preferably volume
3And the settling tank with mud scraper.Along with the raising of biological treatment efficiency, second pond water outlet load can reduce about 47%.
After precipitation process was finished, the waste water after the present invention will precipitate was introduced the dosing reaction tank and is carried out coagulating treatment.In one embodiment of the invention, the volume of described dosing reaction tank is preferably 5000m
3The actual conditions of described coagulating treatment is preferably: temperature is 20 ℃ ~ 35 ℃, is preferably 25 ℃ ~ 30 ℃; The pH value is 6 ~ 8; Hydraulic detention time is 8 hours ~ 12 hours, is preferably 9 hours ~ 11 hours; Adopt this area coagulating agent such as cationic polyacrylamide commonly used to get final product; Dosage of PAC is 3 ‰ ~ 5 ‰.The consumption of the coagulating treatment coagulating agent of the embodiment of the invention significantly reduces, thereby reduces sewage disposal comprehensive cost about 50%.
After coagulating treatment was finished, the COD of the waste water after the coagulating treatment had reached and has entered municipal sewage plant's required standard below 500mg/L, but qualified discharge; The present invention preferably also comprises the mud concentration, precipitating sludge is pumped into sludge thickener together with aerobic excess sludge concentrate, and the mud after concentrating carries out press filtration again to be processed.Wherein, the temperature of described mud concentration is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and hydraulic detention time is 12 hours ~ 16 hours, 2 meters of bandwidth, and the cationic polyacrylamide consumption is 0.3 ‰ ~ 0.5 ‰.It is 1000m that described sludge thickener is preferably volume
3And the sludge thickener with mud scraper.
The technical process of the treatment process of the cotton pulp factory effluent that the embodiment of the invention provides is: waste water → filtration → pH regulator → acidication → degree of depth anaerobic treatment → aerobic aeration → materialization flocculation sediment → qualified discharge.Practice shows that the anaerobism clearance for the treatment of process provided by the invention can maintain more than 60%.The efficient of anaerobic treatment of the present invention is higher, and the load that enters the materialization flocculation process is reduced near 50%, reduces the expense of flocculation medicament, and the biogas amount of generation is increased, and save energy reduces cost.
In order further to understand the present invention, below in conjunction with embodiment the treatment process of anaerobic treatment device provided by the invention and cotton pulp factory effluent is specifically described.
The cotton pulp factory effluent that is 5000mg/L with 10,000 tons of influent load COD filters, and the wire side area of black liquor filter screen is 30m
2, filter screen order number is 100 orders;
Waste water after filtering adds hydrochloric acid, and regulating the pH value is 8.5;
It is 3000m that middle wastewater after the acid adjustment is sent into volume
3The hydrolysis acidification pool processing that is hydrolyzed, processed waste water COD is 4500mg/L, clearance is 10%, wherein, temperature is 30 ℃, sludge concentration is 3g/L, pH is 8.5, hydraulic detention time is 8 hours;
It is 8000m that waste water after the hydrolysis is squeezed into volume with pump
3Anaerobic reactor shown in Figure 1 carry out anaerobic treatment, processed waste water COD is 1800mg/L, clearance is 60%, wherein, temperature is 30 ℃, sludge concentration is 8g/L, pH is 7.5, hydraulic detention time is 18 hours;
To introduce volume through the waste water after the anaerobic treatment is 8000m
3The aerobic aeration pond carry out aerobic treatment, processed waste water COD is 540mg/L, clearance is 65%, wherein, temperature is 28 ℃, sludge concentration is 5g/L, pH is 7.0, hydraulic detention time is 22 hours, dissolved oxygen is 1.0mg/L, reflux ratio is 80%;
It is 3500m that waste water after the aerobic treatment is introduced volume
3And the second pond with mud scraper carries out precipitation process, and treatment condition are: temperature is 30 ℃, and pH is 7.0, and hydraulic detention time is 10 hours;
It is 5000m that waste water after the precipitation is introduced volume
3And the dosing reaction tank with mud scraper carries out coagulating treatment, and processed waste water COD is 270mg/L, and clearance is 60%, and wherein, temperature is 28 ℃, and sludge concentration is 5g/L, and pH is 7.0, and hydraulic detention time is 10 hours, and the cationic polyacrylamide consumption is 4 ‰;
Discharged wastewater met the national standard after the coagulating treatment, and precipitating sludge is pumped into volume together with aerobic excess sludge is 1000m
3And the sludge thickener with mud scraper carries out concentration, and the mud after concentrating carries out press filtration again to be processed.Wherein, the condition of concentration is: temperature is 28 ℃, and sludge concentration is 5g/L, and pH is 7.0, and hydraulic detention time is 14 hours, 2 meters of bandwidth, and the cationic polyacrylamide consumption is 0.4 ‰.
Comparative example 1
Processing step and condition are substantially the same manner as Example 1, and difference is that the cotton pulp factory effluent that is 5000mg/L with 10,000 tons of influent load COD adopts the UASB reactor to carry out anaerobic treatment.Each step water outlet COD is referring to table 1, table 1 be the embodiment of the invention 1 with the method for comparative example 1 in each step water outlet COD contrast.
Each step water outlet COD contrast in the method for table 1 embodiment of the invention 1 and comparative example 1
As shown in Table 1, the anaerobism clearance of the treatment process that the embodiment of the invention provides surpasses 60%, and treatment effect is better.
Simultaneously, the outputted aerobic water COD after comparative example 1 is processed is more than 1000mg/L, if be reduced to below the 500mg/L, the dose that adds coagulating agent needs 1% at least, and the agent of ton water coagulation consumes and needs more than 2 yuan; Even and in the constant situation of the aerobic COD clearance of waste water after processing through embodiment 1, outputted aerobic water COD is near 500mg/L, be reduced to that 500mg/L is following only to need an a small amount of dosing to get final product, therefore, the comprehensive treating process cost savings of embodiment 1 nearly 2 yuan/tons of water.
Processing step and condition are substantially the same manner as Example 1, and difference is, the cotton pulp factory effluent that 10,000 tons of influent load COD are 3000mg/L is processed.
Comparative example 2
Processing step and condition are substantially the same manner as Example 1, and difference is that the cotton pulp factory effluent that is 3000mg/L with 10,000 tons of influent load COD adopts the UASB reactor to carry out anaerobic treatment.Each step water outlet COD is referring to table 2, table 2 be the embodiment of the invention 2 with the method for comparative example 2 in each step water outlet COD contrast.
Each step water outlet COD contrast in the method for table 2 embodiment of the invention 2 and comparative example 2
As shown in Table 2, the anaerobism clearance of the treatment process that the embodiment of the invention provides surpasses 60%, and treatment effect is better.
Processing step and condition are substantially the same manner as Example 1, and difference is, the cotton pulp factory effluent that 10,000 tons of influent load COD are 2000mg/L is processed.
Comparative example 3
Processing step and condition are substantially the same manner as Example 1, and difference is that the cotton pulp factory effluent that is 2000mg/L with 10,000 tons of influent load COD adopts the UASB reactor to carry out anaerobic treatment.Each step water outlet COD is referring to table 3, table 3 be the embodiment of the invention 3 with the method for comparative example 3 in each step water outlet COD contrast.
Each step water outlet COD contrast in the method for table 3 embodiment of the invention 3 and comparative example 3
As shown in Table 3, the anaerobism clearance of the treatment process that the embodiment of the invention provides surpasses 60%, and treatment effect is better.
By above embodiment and comparative example as can be known, the anaerobism clearance of anaerobic treatment is higher in the treatment process of cotton pulp factory effluent provided by the invention, so that cost is lower, is suitable for promoting.
The explanation of above embodiment just is used for helping to understand method of the present invention and core concept thereof.Should be pointed out that for those skilled in the art, under the prerequisite that does not break away from the principle of the invention, can also carry out some improvement and modification to the present invention, these improvement and modification also fall in the protection domain of claim of the present invention.
Claims (10)
1. an anaerobic reactor comprises housing and gas-liquid separator;
Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe;
Described gas-liquid separator communicates with described the first reaction zone by return line.
2. anaerobic reactor according to claim 1 is characterized in that, is provided with annular rising pipe between described the second gas skirt and the described biologic packing material;
The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
3. the treatment process of a cotton pulp factory effluent comprises:
With cotton pulp factory effluent be hydrolyzed successively processing, anaerobic treatment, aerobic treatment and coagulating treatment;
The anaerobic reactor of described anaerobic treatment comprises housing and gas-liquid separator; Described housing is disposed with the first reaction zone, second reaction zone and settling region from top to bottom; Described the first reaction zone bottom is provided with water inlet pipe, and top is provided with the first gas skirt, and described the first gas skirt is communicated with described gas-liquid separator by the biogas-lift pipe; Described second reaction zone top is provided with biologic packing material, and described biologic packing material top is provided with the second gas skirt, and described the second gas skirt is communicated with described gas-liquid separator by effuser; Described settling region is provided with rising pipe; Described gas-liquid separator communicates with described the first reaction zone by return line;
The sludge concentration of described anaerobic treatment is 5g/L ~ 10g/L, and hydraulic detention time is 16 hours ~ 22 hours.
4. treatment process according to claim 3 is characterized in that, is provided with annular rising pipe between described the second gas skirt and the described biologic packing material;
The recycle pump that described anaerobic reactor outer setting has entrance to be communicated with described annular rising pipe, described circulation pump outlet is communicated with described water inlet pipe.
5. treatment process according to claim 3 is characterized in that, the temperature of described anaerobic treatment is 25 ℃ ~ 35 ℃, and the pH value is 6 ~ 8.
6. treatment process according to claim 3 is characterized in that, is hydrolyzed before the processing, and the cotton pulp factory effluent is filtered, and the pH value of the waste water after then will filtering is adjusted to 6 ~ 9.
7. treatment process according to claim 3 is characterized in that, the temperature of described hydrolysis treatment is 25 ℃ ~ 35 ℃, and the pH value is 6 ~ 9, and sludge concentration is 3g/L ~ 6g/L, and hydraulic detention time is 6 hours ~ 10 hours.
8. treatment process according to claim 3 is characterized in that, the temperature of described aerobic treatment is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and sludge concentration is 3g/L ~ 6g/L, and hydraulic detention time is 20 hours ~ 24 hours, and dissolved oxygen is 1.0mg/L ~ 3.0mg/L.
9. treatment process according to claim 3 is characterized in that, after aerobic treatment, before the coagulating treatment, also comprises precipitation process, and the temperature of described precipitation process is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and hydraulic detention time is 8 hours ~ 12 hours.
10. treatment process according to claim 3 is characterized in that, the temperature of described coagulating treatment is 20 ℃ ~ 35 ℃, and the pH value is 6 ~ 8, and hydraulic detention time is 8 hours ~ 12 hours, and dosage of PAC is 3 ‰ ~ 5 ‰.
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| CN112777740A (en) * | 2021-01-29 | 2021-05-11 | 苏州科技大学 | Coal gasification wastewater treatment method and device |
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Application publication date: 20130417 |