CN101811797B - Coal gasification waste water biochemical treatment equipment and method - Google Patents
Coal gasification waste water biochemical treatment equipment and method Download PDFInfo
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- CN101811797B CN101811797B CN 201010121645 CN201010121645A CN101811797B CN 101811797 B CN101811797 B CN 101811797B CN 201010121645 CN201010121645 CN 201010121645 CN 201010121645 A CN201010121645 A CN 201010121645A CN 101811797 B CN101811797 B CN 101811797B
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Abstract
The invention provides coal gasification waste water biochemical treatment equipment and a method. The equipment comprises an anaerobic biochemical treatment unit, an anoxic biochemical treatment unit, a one-grade or multiple-grade aerobic biochemical treatment unit and a membrane biological response unit which are communicated in sequence. In addition, the aerobic biochemical treatment unit is also communicated with the anoxic biochemical treatment unit, and the membrane biological response unit is communicated with the anoxic biochemical treatment unit; each biochemical treatment unit has the characteristics of biochemistry and slurry and water separation integration. The coal gasification waste water biochemical treatment equipment and the method have high COD load and high ammonia nitrogen load and can realize high COD removal rate and high ammonia nitrogen removal rate.
Description
Technical field
The present invention relates to a kind of coal gasification waste water biochemical treatment equipment and method.
Background technology
Coal gasification waste water (comprising coking chemical waste water) is the organic wastewater with difficult degradation thereby of a kind of high COD (chemical oxygen demand (COD)), high ammonia nitrogen.The treatment technology of coal gasification waste water generally is made up of pre-treatment, biochemical treatment, advanced treatment three bulks at present.Biochemical treatment is a main processing mode of removing coal gasification waste water COD, ammonia nitrogen pollutant.Used biochemical processing method mainly is A/O technology (anoxic/aerobic process) and A on coal gasification waste water is handled
2/ O (anaerobism anoxic/aerobic process) technology, SBR technology also has application.The subject matter that existing technology exists is: former water pretreatment is required high, usually need former water is carried out dilution process, COD load and ammonia nitrogen loading are low, the residence time is long, and it is not enough to handle the degree of depth, and COD clearance and ammonia nitrogen removal frank are low, investment and working cost height, subject range to ammonia nitrogen is little, impact capacity is not enough, system's fluctuation of service, and it is very big to handle high ammonia-nitrogen wastewater consumption basicity.
Summary of the invention
The invention provides and a kind ofly have high COD load and high ammonia nitrogen loading, and can realize the coal gasification waste water biochemical treatment equipment and the method for high COD clearance and high ammonia nitrogen removal frank.
In order to solve the problems of the technologies described above, the invention provides following technical scheme:
＜1〉a kind of coal gasification waste water biochemical treatment equipment, described equipment comprise each unit that is communicated with in the following order:
The anaerobic biological processing unit, described anaerobic biological processing unit comprises: the anaerobic biochemical reaction district, wherein carry out anaerobic biochemical reaction to obtain first current with former water in the presence of the active carrier of load anaerobion; And internal circulation system, it is used for the part of first current is recycled to former water;
Anoxic biochemical treatment unit, described anoxic biochemical treatment unit comprises: the anoxic biochemical reaction zone, wherein the another part with first current carries out the anoxic biochemical reaction in the presence of load anoxic microbic activity carrier; And active carrier/moisture abscission zone, it is used for behind the anoxic biochemical reaction active carrier separated with water obtaining second current, and active carrier is turned back in the anoxic biochemical reaction zone;
One or more levels aerobic biochemical processing unit, described aerobic biochemical processing unit comprises: the aerobic biochemical reaction zone, wherein carry out the aerobic biochemical reaction with second current in the presence of the active carrier of load aerobic microbiological; Be used for air is incorporated into device in the aerobic biochemical reaction zone; And active carrier/moisture abscission zone, it is used for after aerobic biochemical reaction active carrier separated with water obtaining the 3rd current, and active carrier is turned back in the aerobic biochemical reaction zone; With
The membrane biological reaction unit, described membrane biological reaction unit comprises: the aerobic biochemical reaction zone, wherein carry out the aerobic biochemical reaction with the part of the 3rd current in the presence of the active carrier of load aerobic microbiological; Be used for air is incorporated into device in the aerobic biochemical reaction zone; Membrane module, it is used for and will carries out membrane filtration to obtain the target current through the part of the current of aerobic biochemical reaction; And active carrier/moisture abscission zone, it is used for carrying out through another part of the current of aerobic biochemical reaction separating obtaining the 4th current of active carrier and water, and active carrier is turned back in the aerobic biochemical reaction zone, and
The aerobic biochemical processing unit is communicated with the anaerobic biological processing unit, be recycled in the anaerobic biological processing unit with another part the 3rd current, and the membrane biological reaction unit is communicated with anoxic biochemical treatment unit, with the 4th water circulation in anoxic biochemical treatment unit.
＜2〉according to＜1〉described coal gasification waste water biochemical treatment equipment, wherein active carrier is a mud.
＜3〉according to＜2〉described coal gasification waste water biochemical treatment equipment, wherein the active carrier in the anoxic biochemical treatment unit/moisture abscission zone comprises: mixed-liquor return district, described mixed-liquor return district are communicated with the anoxic biochemical reaction zone and the active sludge that is used for after the solid-liquid separation turns back to the anoxic biochemical reaction zone; Mud enrichment region, described mud enrichment region are communicated with the mixed-liquor return district and the mud that is used for after the solid-liquid separation accumulates; Solid-liquid displacement zone, described solid-liquid displacement zone and mud enrichment region are communicated with and are used for the solid-liquid separation of active sludge; And clear water zone, described clear water zone is communicated with and is used to collect the water outlet after the solid-liquid separation with the mixed-liquor return district.
＜4〉according to＜3〉described coal gasification waste water biochemical treatment equipment, wherein anoxic biochemical treatment unit also comprises the mixing and stirring system that is used to mix and stir the waste water in the anoxic biochemical reaction zone.
＜5〉according to＜2〉described coal gasification waste water biochemical treatment equipment, wherein active carrier/moisture the abscission zone in the active carrier in the aerobic biochemical processing unit/moisture abscission zone and the membrane biological reaction unit includes: mixed-liquor return district, described mixed-liquor return district are communicated with the aerobic biochemical reaction zone and the active sludge that is used for after the solid-liquid separation turns back to the aerobic biochemical reaction zone; Mud enrichment region, described mud enrichment region are communicated with the mixed-liquor return district and the mud that is used for after the solid-liquid separation accumulates; Solid-liquid displacement zone, described solid-liquid displacement zone and mud enrichment region are communicated with and are used for the solid-liquid separation of active sludge; And clear water zone, described clear water zone is communicated with and is used to collect the water outlet after the solid-liquid separation with the mixed-liquor return district.
＜6〉according to＜2〉described coal gasification waste water biochemical treatment equipment, wherein the anaerobic biological processing unit is a upflow anaerobic sludge blanket process, expanded granular sludge bed or anaerobic fluidized bed.
＜7〉according to＜1〉described coal gasification waste water biochemical treatment equipment, wherein each in anaerobic biological processing unit and the anoxic biochemical treatment unit also is provided with the oxidation reduction potential control instrument in inside, and described oxidation reduction potential control instrument is used for the dissolved oxygen concentration and the recycle ratio of Control Circulation liquid.
＜8〉according to＜1〉described coal gasification waste water biochemical treatment equipment, wherein aerobic biochemical processing unit and membrane biological reaction unit also are provided with the online pH meter of the pH that is used to control waste water.
＜9〉according to＜1〉described coal gasification waste water biochemical treatment equipment, wherein the membrane module in the membrane biological reaction unit is submerged ultrafiltration assembly, plate type membrane assembly or tubular fibre external-compression type membrane module.
＜10〉a kind of coal gasification waste water biochemical processing method said method comprising the steps of:
A. in the anaerobic biochemical reaction district of the active carrier that accommodates the load anaerobion, Jiang Yuanshui carries out anaerobic biochemical reaction obtaining first current, and the part of first current is recycled in the former water;
B. in the anoxic biochemical reaction zone that accommodates load anoxic microbic activity carrier, another part of first current is carried out the anoxic biochemical reaction, active carrier is separated with water obtaining second current, and active carrier is turned back in the anoxic biochemical reaction zone;
C. in the aerobic biochemical reaction zone of the active carrier that accommodates the load aerobic microbiological, under the condition that air is incorporated in the aerobic biochemical reaction zone, second current are carried out the aerobic biochemical reaction, active carrier is separated with water to obtain the 3rd current, and active carrier is turned back in the aerobic biochemical reaction zone, and the part with the 3rd current is recycled in the anaerobic biochemical reaction district simultaneously;
D. in the aerobic biochemical reaction zone of the active carrier that accommodates the load aerobic microbiological, under the condition that air is incorporated in the aerobic biochemical reaction zone, another part of the 3rd current is carried out the aerobic biochemical reaction, the part of reacted current is being carried out membrane filtration with when obtaining the target current then, another part of reacted current is carried out separating to obtain the 4th current of active carrier and water, then active carrier is turned back in the aerobic biochemical reaction zone, and with the 4th water circulation in the anoxic biochemical reaction zone.
＜11〉according to＜10〉described coal gasification waste water biochemical processing method, wherein the active carrier that uses in each step is a mud.
＜12〉according to＜10〉described coal gasification waste water biochemical processing method, wherein the concentration of active carrier is 5000～15000mg/l.
＜13〉according to＜10〉described coal gasification waste water biochemical processing method, wherein with the part of first current with 1: the recycle ratio of 1-3 circulates.
＜14 〉, wherein the part of the 3rd current is circulated with 1: 1～3 recycle ratio according to＜10〉described coal gasification waste water biochemical processing method.
＜15 〉, wherein the part of target current is circulated with 1: 3～5 recycle ratio according to＜10〉described coal gasification waste water biochemical processing method.
＜16〉according to＜13〉or＜14〉described coal gasification waste water biochemical processing method, the wherein dissolved oxygen concentration and the recycle ratio of Control Circulation liquid by the redox potential of Control Circulation liquid.
＜17 〉, wherein in step c and d, control the pH value of second current and the 3rd current by adding alkali according to＜10〉described coal gasification waste water biochemical processing method.
＜18〉according to＜10〉described coal gasification waste water biochemical processing method, wherein in steps d, microbe carrier is added in the part of the 3rd current.
The present invention is the core of waste water biochemical treatment equipment with the high-efficient biological reactor processing unit, the high-efficient biological reactor processing unit has gas, liquid, solid three phase separation 26S Proteasome Structure and Function, the sludge concentration height, airlift circulation and oxygenation, do not need the demoulding device to be set and to reclaim filling carrier as fluidized-bed, complete good mixing effect is to the water quality strong shock resistance.Waste water round-robin between anaerobism, anoxic, aerobic biochemical processing unit flows, active sludge does not participate in circulation, realized the function of nitrification and denitrification equally effectively, because each unitary mud does not mix mutually, therefore each unitary active sludge all has the unique biological feature, show higher activity and efficient, this is and A/O and A
2The part that/O is different, in the present invention anaerobic biological processing unit and A
2There is essential distinction anaerobic treatment unit in the/O technology, and the latter is the purpose for dephosphorization, and the former is the effect for biodegradability that improves hard-degraded substance and removal part ammonia nitrogen.Membrane filtration technique is a kind of new sewage disposal technology, the principal feature of this technology is to substitute traditional gravity solid-liquid separation technique with membrane filtration technique, the efficient height, water quality is good, the present invention receives the membrane biological reaction unit strings after the multi-stage, efficient biochemical treatment unit, mainly be to utilize the lower waste water of membrane biological reaction cell processing substrate concn, keep at reactor under the situation of higher biomass, a lower sludge loading is arranged, be highly effective to the pollution that suppresses film like this, can also be in the membrane biological reaction unit by adding microbe carrier (as bioactive carbon, particulate matter such as flyash), make the microorganism in the membrane biological reaction unit not only have the characteristic of active sludge but also have the biological nature of biomembrance process, can avoid pollution to greatest extent because of membrane module under high-concentration activated sludge and the high matrix condition.
In biochemical processing device of the present invention, the biochemical treatment unit has biochemical and the incorporate characteristics of mud-water separation, active sludge or bio-carrier form self-circulation in the biochemical treatment unit, do not need special mud refluxing unit, can obtain higher activated sludge concentration in biochemical unit, sludge concentration is easy to control, is not subjected to the restriction of mud backflow concentration, sludge age is long especially, and is not subjected to the influence of hydraulic detention time; Each independently can control the important parameters such as concentration, pH value of the dissolved oxygen of processing units at different levels according to the needs of practical situation in the biochemical treatment unit easily and effectively when series connection is used.Efficient biochemical treatment unit has average treatment organic loading height, and compact construction, does not need mud refluxing unit, reduced investment, control and management characteristic of simple at the sludge concentration height.
Therefore, biochemical combined treatment process of the present invention has the adaptability and the impact resistance of high COD, high ammonia-nitrogen wastewater, can tolerate the high-concentration coal gasification waste water that water inlet COD5000mg/l is above, ammonia nitrogen reaches 900mg/l, can reach the COD clearance greater than 93%, ammonia nitrogen removal frank is greater than 99% treatment effect.
Therefore, this biochemical process combination various high ammonia nitrogen, difficult degradation, low C/N of being suitable for comprising coal gasification waste water than, can biochemical Industrial Wastewater Treatment.
Description of drawings
Fig. 1 is the general illustration according to the coal gasification waste water biochemical treatment equipment of one embodiment of the invention;
Fig. 2 is the synoptic diagram of the anaerobic biological processing unit in the present device;
Fig. 3 is the unitary synoptic diagram of anoxic biochemical treatment in the present device;
Fig. 4 is the synoptic diagram of the aerobic biochemical processing unit in the present device;
Fig. 5 is the unitary synoptic diagram of the membrane biological reaction in the present device.
Embodiment
Waste water biochemical treatment equipment of the present invention comprises anaerobic biological processing unit, anoxic biochemical treatment unit, aerobic biochemical processing unit and membrane biological reaction unit.According to concrete water quality treatment, the aerobic biochemical processing unit can be one-level, two-stage or three grades, is preferably more than the two-stage.
Fig. 1 is the figure that shows as a preferred embodiment of waste water biochemical treatment equipment of the present invention.As shown in Figure 1, waste water biochemical treatment equipment of the present invention comprises anaerobic biological processing unit 1, anoxic biochemical treatment unit 2, one-level aerobic biochemical processing unit 3, secondary aerobic biochemical processing unit 4 and membrane biological reaction unit 5.The concrete structure of each component units will be described respectively below.
The anaerobic biological processing unit
In the present invention, the anaerobic biological processing unit can be UASB (upflow anaerobic sludge blanket process), the EGSB (expanded granular sludge bed) or anaerobic fluidized bed of routine.
Fig. 2 is the structural representation of anaerobic biological processing unit of the present invention (UASB).
Anaerobic biological processing unit 1 of the present invention can be square or round, can be that steel, glass reinforced plastic or concrete placement form.
Into water water distribution system 2, anaerobic sludge layer 3, supernatant liquid zone 4, internal circulation system 5, oxidation reduction potential control instrument 6 are arranged in the anaerobic biological processing unit.
The anaerobic sludge layer 3 of anaerobic biological processing unit is the main reaction region of anaerobic biological, under the effect of this reaction zone anaerobion, the larger molecular organics hydrolysis of bio-refractory is become the small-molecule substance of easy degraded, have part nitrite and ammonia under action of microorganisms, to comprise the anaerobic biochemical reaction of Anammox reaction simultaneously.The water inlet of former water with enter into water water distribution system 2 after supernatant liquor recirculated water and aerobic biochemical cycle of treatment water mix, pass anaerobic sludge layer 3 equably, finish the current rising of anaerobic biological processing back and enter clear water zone, an ascending current part enters internal circulation system 5, another part enters next stage anoxic biochemical treatment unit, the concentration and the recycle ratio of redox potential height in the oxidation reduction potential control instrument 6 main indication anaerobic biological processing units and control I and II aerobic biochemical reaction member circulation fluid dissolved oxygen.
Anoxic biochemical treatment unit
Fig. 3 is the unitary structural representation of anoxic biochemical treatment of the present invention.
Anoxic biochemical treatment of the present invention unit 1 can be square or circular, and can be that steel, glass reinforced plastic or concrete placement form.Can be filled with active sludge (being the microorganism micelle) in the anoxic biochemical treatment unit 1; also can be filled with flowable biologic packing material carrier (as plastics porous ball, granulated active carbon), active sludge or biologic packing material carrier are the carriers of load microbial growth.The unitary middle part of anoxic biochemical treatment is an anoxic biochemical reaction zone (denitrification zone) 2, is the main reaction region of denitrification denitrogenation, and anoxic mud load anaerobion is mainly based on denitrifying bacteria.
The lopsidedness ground of inside, anoxic biochemical treatment unit forms a mixed-liquor return district 3 to having a reflux guide plate 10, and the mud after the solid-liquid separation is brought back to denitrification zone.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 water surface of denitrification zone 2, and the lower end of this reflux guide plate 10 is provided with mixed-liquor return seam 11 and is communicated with denitrification zone 2, guarantees that stirring generation mixed solution circulates.
Between the sidewall of reflux guide plate 10 and anoxic biochemical treatment unit 1, tilt down to be provided with a mud and separate plate 7, form a mud enrichment region 6, mainly accumulate the active sludge after the solid-liquid separation; This mud separates plate 7 and can adopt steel, PVC, ABS, glass reinforced plastic or concrete placement to form.The lower end that this mud separates plate 7 has reflux seam 8 of a mud to be communicated with denitrification zone 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, realize the purpose of solid-liquid separation, and this solid-liquid displacement zone 5 is equipped with swash plate or inclined tube filler, 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 rising pipe 14; The effluent adopting overflow weir of clear water zone 4 or submerged water gathering system, submerged water gathering system adopt symmetrical reversed return type design.Clear water zone 4 and mud enrichment region 6 separate plate 7 by settling region dividing plate 9, mud respectively isolates with denitrification zone, and the bottom in the bottom of mud enrichment region 6 and mixed-liquor return district 3 is communicated with denitrification zone 2, but get back in the denitrification zone 2 for ease of active sludge or flowing carrier, below corresponding mud backflow seam 8, locate to be provided with oblique slip plate 13.
The unitary central authorities of anoxic biochemical treatment are provided with mixing agitator 12, and this agitator is by electric motor driving.
Process when anoxic biochemical treatment of the present invention unit (see figure 3) is carried out wastewater treatment is, the water outlet of anaerobic pond enters the denitrification zone 2 of anoxic biochemical treatment unit 1, under the stirring action of agitator 12, to intake rapidly to mix and finish denitrification process with the unitary backflow supernatant liquor of membrane biological reaction, the mixed solution of denitrification zone enters mud enrichment region 6 by mud backflow seam 8 under the power that stirs, 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 denitrification 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 passes through solid-liquid displacement zone 5, the water gathering system 14 that enters clear water zone 4, and supernatant liquor enters next stage biochemical treatment unit by water gathering system 14.In addition, anoxic biochemical treatment unit is provided with the oxidation reduction potential control instrument in inside, and described oxidation reduction potential control instrument is used for the dissolved oxygen concentration and the recycle ratio of Control Circulation liquid.
The aerobic biochemical processing unit
Fig. 4 is the structural representation of aerobic biochemical processing unit device of the present invention.
Aerobic biochemical processing unit device of the present invention can be square or circular, and can be that steel, glass reinforced plastic or concrete placement form.Be filled with active sludge in the biochemical treatment apparatus, also can be filled with flowable biologic packing material carrier.Microorganism in the aerobic biochemical processing units at different levels is aerobic microbiological, can be substantially the same or slightly different according to water quality, for example, microorganism in the one-level aerobic biochemical processing unit can mainly be to be the heterotrophism flora of matrix with the carbon source, and the microorganism part in the secondary aerobic biochemical processing unit can be to be that the heterotrophic bacterium and the part of matrix is the autotrophy nitrifier of matrix with the ammonia nitrogen with the carbon source.
The middle part of aerobic biochemical processing unit device is aerobic aeration district 2, is the main reaction region of biochemical treatment; The lopsidedness ground of biochemical treatment apparatus inside forms a mixed-liquor return district 3 to having a reflux guide plate 10, and the mud after the solid-liquid separation is brought back to the aerobic aeration district.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 water surface 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 aerobic biochemical processing unit device 1, tilt down to be provided with a mud and separate plate 7, form a mud enrichment region 6, mainly accumulate the active sludge after the solid-liquid separation; This mud separates plate 7 and can adopt steel, PVC, ABS, glass reinforced plastic or concrete placement to form.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, are used to realize the purpose of solid-liquid separation, and this solid-liquid displacement zone 5 is equipped with swash plate or inclined tube filler, 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, submerged water gathering system to adopt symmetrical reversed return type design.Clear water zone 4 and mud enrichment region 6 separate plate 7 by precipitation dividing plate 9, mud respectively isolates with the 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, locate to be provided with oblique slip plate 13.
The bottom of aerobic biochemical processing unit device 1 is provided with aerator 12, and this aerator 12 connects an inlet pipe.The form of aerator can be micro-hole aerator, micropore aeration pipe or perforated pipe.
Process when aerobic biochemical processing unit device of the present invention carries out wastewater treatment is, waste water enters the aerobic aeration district 2 of biochemical treatment apparatus 1, under the aeration effect of aerator 12, to intake rapidly with biochemical treatment apparatus 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.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 membrane biological reaction unit
Fig. 5 is the unitary structural representation of membrane biological reaction of the present invention.
Membrane biological reaction of the present invention unit 1 can be square or circular, and can be that steel, glass reinforced plastic or concrete placement form.Be filled with active sludge in the biochemical treatment apparatus 1, also can be filled with flowable biologic packing material carrier.The unitary microorganism of membrane biological reaction also is an aerobic microbiological, according to water quality, can be substantially the same with the microorganism in the aerobic biochemical processing unit or slightly different, for example, the major microorganisms flora in the reactor can be made up of the autotrophy nitrifier that with the ammonia nitrogen is matrix.
The unitary middle part of membrane biological reaction is aerobic aeration district 2, is the main reaction region of biochemical treatment; The lopsidedness ground of biochemical treatment apparatus inside forms a mixed-liquor return district 3 to having a reflux guide plate 10, and the mud after the solid-liquid separation is brought back to the aerobic aeration district.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 water surface 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 treatment apparatus 1, tilt down to be provided with a mud and separate plate 7, form a mud enrichment region 6, mainly accumulate the active sludge after the solid-liquid separation; This mud separates plate 7 and can adopt steel, PVC, ABS, glass reinforced plastic or concrete placement to form.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, realize the purpose of solid-liquid separation, and this solid-liquid displacement zone 5 is equipped with swash plate or inclined tube filler, 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, submerged water gathering system to adopt symmetrical reversed return type design.Clear water zone 4 and mud enrichment region 6 separate plate 7 by precipitation dividing plate 9, mud respectively isolates with the 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, locate to be provided with oblique slip plate 13.
The bottom of membrane biological reaction unit 1 is provided with aerator 12, and this aerator 12 connects an inlet pipe.The form of aerator can be micro-hole aerator, micropore aeration pipe or perforated pipe.
Process when membrane biological reaction of the present invention unit carries out wastewater treatment is, waste water enters the aerobic aeration district 2 of membrane biological reaction unit 1, under the aeration effect of aerator 12, to intake rapidly with biochemical treatment apparatus 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 finish water after nitrated by solid-liquid displacement zone 5, and the water gathering system 14 that enters clear water zone 4, supernatant liquor is back to the anoxic bio-reactor by water gathering system 14 and carries out denitrification under the lifting of system's reflux pump.
The treat effluent of total system is that the membrane module 15 by being located at aeration zone 2 carries out membrane filtration with the mixed solution in aerobic aeration district 2, extracts the processing that treating water are finished whole biochemistry out by suction pump 16.
Can also be in the membrane biological reaction unit by adding microbe carrier (as particulate matter such as bioactive carbon, flyash), make the microorganism in the membrane biological reaction unit not only have the characteristic of active sludge but also have the biological nature of biomembrance process, can avoid pollution to greatest extent because of membrane module under high-concentration activated sludge and the high matrix condition.
Consult Fig. 1 once more, the water inlet of former water is connected on the rising pipe of internal recycle recycle pump 6 of anaerobic biological processing unit, the treating water of one-level aerobic biochemical is by the top suction of recycle pump 7 from one-level aerobic biochemical processing unit, also import on the rising pipe of internal recycle recycle pump 6 of anaerobic biological processing unit, the internal recycle recycle pump 6 of anaerobic biological processing unit extracts supernatant liquor from the top of anaerobic biological processing unit, send into the bottom water distributor of anaerobic biological processing unit after on its rising pipe three strands of current being confluxed; The rising pipe of anaerobic biological processing unit 1 is located at top, the rising pipe the other end is connected the unitary bottom of anoxic biochemical treatment, the unitary supernatant liquor of membrane biological reaction also arrives the unitary bottom of anoxic biochemical treatment by recycle pump 8, and the water absorption tube of recycle pump 8 is arranged on the unitary top of membrane biological reaction; The unitary supernatant liquor of anoxic biochemical treatment is by the bottom that water pipe is connected to one-level aerobic biochemical processing unit that overflows on top, the supernatant liquor of one-level aerobic biochemical processing unit is connected to the bottom of secondary aerobic biochemical processing unit by the upflow tube that is located at top, and the supernatant liquor of secondary aerobic biochemical processing unit is connected to the unitary bottom of membrane biological reaction by upflow tube; The treating water of biochemistry combination process of the present invention is extracted out by suction pump 9, and the water absorption tube of suction pump 9 is connected on the rising pipe of membrane module; Blower conduits is connected respectively to the aerating system of I and II aerobic biochemical processing unit and membrane biological reaction unit bottom.
The present invention is used to handle high COD, high ammonia-nitrogen wastewater is the biochemical treatment combination process of the coal gasification waste water (comprising coking chemical waste water) of feature.The suitable pre-treatment of coal gasification waste water process (COD does not limit, volatile phenol＜1500mg/L, ammonia nitrogen＜1000mg/L, the content＜40mg/L of tar and oil 〉.After coal gasification waste water process oil removal and oil removal by air bubbling satisfy the needs of biochemical treatment, directly send into the bottom of anaerobic biological processing unit with intake pump, the temperature maintenance of anaerobic biological processing unit is between 25～35 ℃, sludge concentration is more than 10000mg/l, hydraulic detention time 24 hours, the supernatant liquor of influent waste water and anaerobic biological processing unit and mix from the circulation fluid of secondary aerobic biochemical processing unit after, pass the top that the anaerobic sludge layer rises to anaerobic reactor from the bottom of anaerobic biological processing unit, enter anoxic biochemical treatment unit 2 through the water gravity overflow after the anaerobic treatment, supernatant liquor in the membrane biological reaction unit is recycled to anoxic biochemical treatment unit 2 by denitrification internal circulation pump 8 simultaneously, in the anoxic biochemical treatment unit 2 mixed stirring device is set, stirring intensity is 5～20W, temperature maintenance normal temperature, be not less than 20 ℃, water inlet and circulation fluid stopped 8～12 hours in anoxic biochemical treatment unit 2, waste water and circulation fluid are after this district finishes denitrification process, solid-liquid displacement zone through anoxic biochemical treatment unit 2 enters efficient biochemical treatment unit---one-level aerobic biochemical processing unit 3, efficient biochemical treatment unit---be provided with micro-hole aerator in the one-level aerobic biochemical processing unit 3, by gas blower to its oxygenation, dissolved oxygen concentration is not less than 2mg/l, temperature is not less than 20 ℃, hydraulic detention time was at 12～30 hours, flow into efficient biochemical treatment unit through waste water gravity behind the solid-liquid separation unit in the reactor---secondary aerobic biochemical processing unit 4, efficient biochemical treatment unit---be provided with micro-hole aerator in the secondary aerobic biochemical processing unit 4, by gas blower to its oxygenation, dissolved oxygen concentration is not less than 2mg/l, the pH value adds alkali by online pH meter control, maintain between the 7.2-8.2, temperature is not less than 20 ℃, hydraulic detention time was at 12-30 hour, enter membrane biological reaction unit 5 through waste water gravity behind the solid-liquid separation unit in the reactor, be provided with micro-hole aerator and hyperfiltration membrane assembly in the membrane biological reaction unit 5, by gas blower to its oxygenation, dissolved oxygen concentration is not less than 2mg/l, the pH value adds alkali by online pH meter control, maintain between the 7.2-8.2, temperature is not less than 20 ℃, hydraulic detention time was finished biochemical treatment water outlet through the membrane module in the reactor by film water outlet suction pump 9 suctions at 12～30 hours.
In aeration process, gas-water ratio is 50～100.Gas-water ratio is meant that processing waste water per ton need provide the air capacity under the standard pressure, and air capacity, is meant and handles 1 ton of water, 100 cubic metres of the air that the consumption mark is depressed as gas-water ratio 100 in cubic meter.
Mud cake was inoculated after the unitary mud of each biochemical treatment was used sludge from wastewater treatment plant concentration basin mud or press filtration, and inoculation back mixed solution sludge concentration is not less than 1000mg/L.Activated sludge concentration is respectively: the anaerobic biological processing unit is＞10000mg/L, anoxic biochemical treatment unit is＞5000mg/L, one-level aerobic biochemical processing unit is＞5000mg/L that secondary aerobic biochemical processing unit is＞5000mg/L that the membrane biological reaction unit is＞5000mg/L.
Waste water has three circulations, and first circulation is that the supernatant liquor in the anaerobic biological processing unit enters the bottom water distributor of anaerobic biological processing unit after mixing by anaerobism recycle pump 6 and water inlet, and recycle ratio is 1: 1～3; Second circulation is efficient biochemical treatment unit---the supernatant liquor of secondary aerobic biochemical processing unit is recycled to the anaerobic biological processing unit by Anammox recycle pump 7, and recycle ratio is 1: 1～3; The 3rd circulation is that the supernatant liquor of the solid-liquid displacement zone of membrane biological reaction unit 5 is recycled to anoxic biochemical treatment unit 2 by the denitrification internal circulation pump, and recycle ratio is 1: 3～5; The different differences that are supernatant liquor and mixed solution of these three circulations and the reflux cycle maximum of other technology, the independent operating of mud and water just makes the present invention have unique treatment effect and efficient just.High sludge quantity, the unitary series operation of multi-stage, efficient biochemical treatment are the important technology features of efficient biochemistry combination process of the present invention.
Adopt combination process of the present invention that coal gasification waste water is handled, the result is as follows.
Certain actual coal gasification waste water water inlet COD:8600mg/l; Influent ammonia nitrogen: 893.41mg/l; Water inlet volatile phenol: 1530mg/l; Sulfide: 70mg/l, biochemical treatment total residence time 80 hours (wherein 15 hours anaerobic biological processing unit residence time, 12 hours anoxic biochemical treatment unit residence time, 20 hours one-level aerobic biochemical processing unit residence time, secondary aerobic biochemical processing unit stop 20 hours, 13 hours membrane biological reaction unit residence time), activated sludge concentration average out to: 6000mg/l, gas-water ratio 100, the pH value maintains between 7.2～7.7 always, and waste water has obtained the treatment effect shown in the table 1 always under the condition more than 20 ℃.
Table 1
| Water-quality guideline | Former water | The water outlet of anaerobic biological processing unit | Anoxic biochemical treatment unit water outlet | The water outlet of one-level aerobic biochemical processing unit | The water outlet of secondary aerobic biochemical processing unit | The water outlet of membrane biological reaction unit |
| COD(mg/L) | 8600 | 8346 | 1524 | 840 | 563 | 284 |
| Ammonia nitrogen (mg/L) | 893.41 | 868.46 | 241.77 | 127.72 | 44.2 | 0 |
| Volatile phenol (mg/L) | 1530 | 1431 | 346 | 148 | 23 | 0 |
| Sulfide (mg/L) | 70 | 73 | 24 | 12 | 0 | 0 |
At the former water COD of water inlet, ammonia nitrogen, Pollutant levels such as volatile phenol are high waste water so, processing through coal gasification waste water biochemical treatment equipment of the present invention, be issued to very high processing horizontal in 80 hours condition of total hrt, especially ammonia-N removal rate is very high, so high ammonia nitrogen does not produce restraining effect to whole biochemical system, mainly be because the efficient biochemical unit complete blended efficient height of this technology, and the circulation of supernatant liquor, the anaerobic biological water outlet enters the biochemical section of anoxic and is diluted fast, has greatly alleviated the restraining effect of toxic substance.Because the microorganism feature of biochemical sections at different levels is obvious, sludge quantity is bigger, makes the processing of each biochemical stage load far above A/O and A
2/ O technology, the average COD load has reached 1kg/m
3More than the d, ammonia nitrogen loading reaches 0.26kg/m
3D, and A/O and A
2The average COD load of/O technology has only 0.3～0.5kg/m
3D, ammonia nitrogen loading has only 0.1kg/m
3About d.Coal gasification waste water biochemical processing process of the present invention is handled adaptation concentration to ammonia nitrogen considerably beyond existing treatment process level (in the 200mg/l).
Biochemical combined treatment process of the present invention has the adaptability and the impact resistance of high COD, high ammonia-nitrogen wastewater, can tolerate the high-concentration coal gasification waste water that water inlet COD5000mg/l is above, ammonia nitrogen reaches 900mg/l, can reach the COD clearance greater than 93%, ammonia nitrogen removal frank is greater than 99% treatment effect.
Claims (18)
1. coal gasification waste water biochemical treatment equipment, described equipment comprise each unit that is communicated with in the following order:
The anaerobic biological processing unit, described anaerobic biological processing unit comprises: the anaerobic biochemical reaction district, wherein carry out anaerobic biochemical reaction to obtain first current with former water in the presence of the active carrier of load anaerobion; And internal circulation system, it is used for the part of first current is recycled to former water;
Anoxic biochemical treatment unit, described anoxic biochemical treatment unit comprises: the anoxic biochemical reaction zone, wherein the another part with first current carries out the anoxic biochemical reaction in the presence of load anoxic microbic activity carrier; And active carrier/moisture abscission zone, it is used for behind the anoxic biochemical reaction active carrier separated with water obtaining second current, and active carrier is turned back in the anoxic biochemical reaction zone;
One or more levels aerobic biochemical processing unit, described aerobic biochemical processing unit comprises: the first aerobic biochemical reaction zone, wherein carry out the aerobic biochemical reaction with second current in the presence of the active carrier of load aerobic microbiological; Be used for air is incorporated into device in the first aerobic biochemical reaction zone; And active carrier/moisture abscission zone, it is used for after aerobic biochemical reaction active carrier separated with water obtaining the 3rd current, and active carrier is turned back in the first aerobic biochemical reaction zone; With
The membrane biological reaction unit, described membrane biological reaction unit comprises: the second aerobic biochemical reaction zone, wherein carry out the aerobic biochemical reaction with the part of the 3rd current in the presence of the active carrier of load aerobic microbiological; Be used for air is incorporated into device in the second aerobic biochemical reaction zone; Membrane module, it is used for and will carries out membrane filtration to obtain the target current through the part of the current of aerobic biochemical reaction; And active carrier/moisture abscission zone, it is used for carrying out through another part of the current of aerobic biochemical reaction separating obtaining the 4th current of active carrier and water, and active carrier is turned back in the second aerobic biochemical reaction zone, and
The aerobic biochemical processing unit is communicated with the anaerobic biological processing unit, be recycled in the anaerobic biological processing unit with another part the 3rd current, and the membrane biological reaction unit is communicated with anoxic biochemical treatment unit, with the 4th water circulation in anoxic biochemical treatment unit.
2. coal gasification waste water biochemical treatment equipment according to claim 1, wherein active carrier is a mud.
3. coal gasification waste water biochemical treatment equipment according to claim 2, wherein the active carrier in the anoxic biochemical treatment unit/moisture abscission zone comprises: mixed-liquor return district, described mixed-liquor return district are communicated with the anoxic biochemical reaction zone and the active sludge that is used for after the solid-liquid separation turns back to the anoxic biochemical reaction zone; Mud enrichment region, described mud enrichment region are communicated with the mixed-liquor return district and the mud that is used for after the solid-liquid separation accumulates; Solid-liquid displacement zone, described solid-liquid displacement zone and mud enrichment region are communicated with and are used for the solid-liquid separation of active sludge; And clear water zone, described clear water zone is communicated with and is used to collect the water outlet after the solid-liquid separation with the mixed-liquor return district.
4. coal gasification waste water biochemical treatment equipment according to claim 3, wherein anoxic biochemical treatment unit also comprises the mixing and stirring system that is used to mix and stir the waste water in the anoxic biochemical reaction zone.
5. coal gasification waste water biochemical treatment equipment according to claim 2, wherein active carrier/moisture the abscission zone in the active carrier in the aerobic biochemical processing unit/moisture abscission zone and the membrane biological reaction unit includes: mixed-liquor return district, described mixed-liquor return district are communicated with the aerobic biochemical reaction zone and the active sludge that is used for after the solid-liquid separation turns back to the aerobic biochemical reaction zone; Mud enrichment region, described mud enrichment region are communicated with the mixed-liquor return district and the mud that is used for after the solid-liquid separation accumulates; Solid-liquid displacement zone, described solid-liquid displacement zone and mud enrichment region are communicated with and are used for the solid-liquid separation of active sludge; And clear water zone, described clear water zone is communicated with and is used to collect the water outlet after the solid-liquid separation with the mixed-liquor return district.
6. coal gasification waste water biochemical treatment equipment according to claim 2, wherein the anaerobic biological processing unit is a upflow anaerobic sludge blanket process, expanded granular sludge bed or anaerobic fluidized bed.
7. coal gasification waste water biochemical treatment equipment according to claim 1, wherein each in anaerobic biological processing unit and the anoxic biochemical treatment unit also is provided with the oxidation reduction potential control instrument in inside, and described oxidation reduction potential control instrument is used for the dissolved oxygen concentration and the recycle ratio of Control Circulation liquid.
8. coal gasification waste water biochemical treatment equipment according to claim 1, wherein aerobic biochemical processing unit and membrane biological reaction unit also are provided with the online pH meter of the pH that is used to control waste water.
9. coal gasification waste water biochemical treatment equipment according to claim 1, wherein the membrane module in the membrane biological reaction unit is submerged ultrafiltration assembly, plate type membrane assembly or tubular fibre external-compression type membrane module.
10. coal gasification waste water biochemical processing method said method comprising the steps of:
A. in the anaerobic biochemical reaction district of the active carrier that accommodates the load anaerobion, Jiang Yuanshui carries out anaerobic biochemical reaction obtaining first current, and the part of first current is recycled in the former water;
B. in the anoxic biochemical reaction zone that accommodates load anoxic microbic activity carrier, another part of first current is carried out the anoxic biochemical reaction, active carrier is separated with water obtaining second current, and active carrier is turned back in the anoxic biochemical reaction zone;
C. in the first aerobic biochemical reaction zone of the active carrier that accommodates the load aerobic microbiological, under the condition in air being incorporated into the first aerobic biochemical reaction zone, second current are carried out the aerobic biochemical reaction, active carrier is separated with water to obtain the 3rd current, and active carrier is turned back in the first aerobic biochemical reaction zone, and the part with the 3rd current is recycled in the anaerobic biochemical reaction district simultaneously;
D. in the second aerobic biochemical reaction zone of the active carrier that accommodates the load aerobic microbiological, under the condition in air being incorporated into the second aerobic biochemical reaction zone, another part of the 3rd current is carried out the aerobic biochemical reaction, the part of reacted current is being carried out membrane filtration with when obtaining the target current then, another part of reacted current is carried out separating to obtain the 4th current of active carrier and water, active carrier is turned back in the second aerobic biochemical reaction zone then, and with the 4th water circulation in the anoxic biochemical reaction zone.
11. coal gasification waste water biochemical processing method according to claim 10, wherein the active carrier that uses in each step is a mud.
12. coal gasification waste water biochemical processing method according to claim 10, wherein the concentration of active carrier is 5000～15000mg/l.
13. coal gasification waste water biochemical processing method according to claim 10 wherein circulates the part of first current with 1: 1～3 recycle ratio.
14. coal gasification waste water biochemical processing method according to claim 10 wherein circulates the part of the 3rd current with 1: 1～3 recycle ratio.
15. coal gasification waste water biochemical processing method according to claim 10 wherein circulates the part of target current with 1: 3～5 recycle ratio.
16. according to claim 13 or 14 described coal gasification waste water biochemical processing methods, the wherein redox potential by Control Circulation liquid and the dissolved oxygen concentration and the recycle ratio of Control Circulation liquid.
17. coal gasification waste water biochemical processing method according to claim 10 is wherein controlled the pH value of second current and the 3rd current by adding alkali in step c and d.
18. coal gasification waste water biochemical processing method according to claim 10 wherein is added to microbe carrier in steps d in the part of the 3rd current.
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