CN105293607B - Purine produces the processing method of waste water - Google Patents
Purine produces the processing method of waste water Download PDFInfo
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- CN105293607B CN105293607B CN201410331819.6A CN201410331819A CN105293607B CN 105293607 B CN105293607 B CN 105293607B CN 201410331819 A CN201410331819 A CN 201410331819A CN 105293607 B CN105293607 B CN 105293607B
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Abstract
The present invention relates to the processing method that a kind of purine produces waste water, after the amination that is produced in purine production process, cyclization, three bursts of sewage mixing of purine, carry out air-distillation, distill out light component, the vacuum distillation under vacuum after tower reactor is cooled to 67 70 DEG C after air-distillation, aqueous phase is steamed, raffinate discharge distillation still is burned after being mixed with the light component steamed, steams aqueous phase and post-processed.Economical rationality of the present invention, simple to operate, technical feasibility, it is easy to operate, wastewater toxicity can be effectively reduced, waste water COD is reduced, NH is reduced3N etc. content, finally makes water outlet can reach the receiving requirement of sewage plant.
Description
Technical field
The present invention relates to a kind of processing method of disposal of industrial wastewater, and in particular to a kind of purine produces the processing side of waste water
Method.
Background technology
With China's rapid development of economy, water pollution is also on the rise, especially to high concentration hard-degraded organic waste water
Administer and control has turned into the problem that field of environment engineering is faced jointly.Waste water containing hardly degraded organic substance, which is referred to as difficult degradation, to be had
Machine waste water, hardly degraded organic substance refers to degrade in microorganism, or can not be dropped under any environmental condition with enough speed
The compound for solving and making it accumulate in the environment.The species of high-concentration hardly-degradable compound is a lot, generally according to organic compound
Structure and characteristic, persistent organic pollutant wastewater can be divided into polycyclic aromatic compounds, heterocycle compound, chlorination virtue
Fragrant compounds of group, organic cyanide, organic synthesis high-molecular compound etc..Because biodegradable organic compoundses are difficult by microorganism
Degraded, they necessarily not easily pass through most popular biological treatment at present and removed, are discharged into the natural environments such as water body
It is not easy to gradually decrease its content by natural self purification.Therefore, they can be in the natural mediums such as water body, soil not
Disconnected accumulation, breaks original balance of the ecosystem, huge threat is caused to environment for the survival of mankind, and it can pass through food
Thing chain enters organism and is progressively enriched with, and finally enters human body, is detrimental to health.
At present, persistent organic pollutant wastewater treatment technology uses biological treatment mostly, but due to a large amount of in waste water
The presence of persistent organic pollutants, it is difficult to prove effective to often lead to conventional biological treatment, and persistent organic pollutants are not
Can effectively it degrade, the draining after processing can not reach all kinds of defined discharge standards, so as to cause whole sewage treatment project not have
Have and reach expected purpose.Therefore to the understanding of persistent organic pollutants water quality and correct handling process is selected to be very must
Want.
Tan Jing etc. is in " the biological treatment engineering practice of xanthine drug synthetic wastewater " from anaerobic baffle plate reaction
Device (ABR)-efficient aeration pool technique, introduces EMO composite flora technologies, handles xanthine medicine series waste water, in water inlet
Under the conditions of COD8000-10000mg/L higher load, water outlet COD≤500mg/L, COD clearance is up to more than 90%.The work
Skill have the advantages that simple to operate, small investment, impact resistance, operate steadily, operate it is flexible.
Hu Wenwei etc. describes a kind of processing method of use materialization+biochemistry in " guanine produces the processing of waste water " text
Handle the handling process that guanine produces waste water, COD and NH3The guanine that-N is up to 40000mg/L and 2400mg/L respectively gives up
Water first passes around the pretreatment of stripping deamination, then adjusts water quality with low concentration wastewater, then through hydrolysis in 10 hours, 10 hours contact oxygen
It is 130-150mg/L, NH3-N≤25mg/L to change final outflow water CODcr.Sludge produced by guanine sewage disposal send Bricks and Tiles Plant
Brickmaking.
Sewage handled by two more closely related documents of the above is xanthine pharmaceutical synthesis waste water and guanine life respectively
Waste water is produced, the water quality of the serial waste water of purine production handled with the present invention is widely different.Purine in the serial waste water of purine production
Waste water, cyclization waste water and amination waste water COD contents are up to 200000-360000mg/L, 8100mg/L and 4600mg/L, ring respectively
Close waste water and amination waste water and also contain high inorganic salts and high ammonia nitrogen respectively, its intractability is far above above-mentioned document institute
It is related to the difficulty of waste water.Literature survey shows that producing waste water to purine, there is presently no corresponding processing means.
Certain enterprise produces 24t purine products per year, is produced using intermittent feeds mode, and sewage intermittent discharge is collected, sewage
Total amount is about 1m3/ days.Purine production process is broadly divided into cyclization, amination, 3 steps of purine, and accordingly produces 3 strands of sewage.3
Stock sewage quality is widely different, and amination sewage contains 2.8% NH3-N；Purine COD of sewage is up to 300000mg/L, cyclization dirt
Water conductivity is up to 600000 μ S/cm.In a word, the serial sewage of purine production is the generally acknowledged difficult sewage of industry, with height
The characteristics of COD, high NH3-N, high salt, high Cl-, difficult for biological degradation, big toxicity.The process object of the present invention is high COD, high saliferous
Purine produced in series sewage, the sewage has penetrating odor, and toxicity is big, it is difficult to biochemical treatment, using Fenton reagent etc.
Reoxidized after advanced oxidation processes direct oxidation or dilution be also difficult to be processed to it is up to standard.
The content of the invention
It is an object of the invention to provide the processing method that a kind of purine produces waste water, economical rationality, simple to operate, technology can
Capable handling process, it is easy to operate, wastewater toxicity can be effectively reduced, waste water COD is reduced, NH is reduced3- N etc. content, finally
Water outlet is set to can reach the receiving requirement of sewage plant.
A kind of purine of the present invention produce the amination produced in the processing method of waste water, purine production process, cyclization,
After three bursts of sewage mixing of purine, air-distillation is carried out, light component is distilled out, after air-distillation after tower reactor is cooled to 67-70 DEG C
Vacuum distillation under vacuum, steams aqueous phase, and raffinate discharge distillation still is burned after being mixed with the light component steamed, steams aqueous phase
Post-processed.
The amination that is produced in purine production process, cyclization, the mol ratio of three strands of sewage of purine are 0.7：1：1.
The destilling tower number of plates is 4-10 blocks.It is preferred that 6-9 blocks.
Air-distillation steams the ratio 6%-12% of light component, preferably 9%-11%；Vacuum distillation vacuum 0.05-
0.08Mpa, preferably 0.06-0.07Mpa；Steam watr-proportion 50%-70%, preferably 58%-62%.
During the air-distillation for steaming light component, temperature is 88-90 DEG C when mixed liquor seethes with excitement；Light component condensation discharging
When, bottom temperature is 96-98 DEG C, and tower top temperature is 76-78 DEG C；At the end of steaming light component, bottom temperature is 101-103 DEG C,
Tower top temperature is 90-100 DEG C.
Boiling temperature is 71-73 DEG C during vacuum distillation, when overhead condensation discharges, and bottom temperature is 73 DEG C, and tower top temperature is
68℃；When steaming the completion of 60% aqueous phase, bottom temperature is 79 DEG C, and tower top temperature is 69.5 DEG C.
The treatment effect that the process conditions of distillation technique produce waste water to purine has a direct impact.
The aqueous phase post-processing step that vacuum distillation goes out is：COD contents produce for 500-700mg/L wastewater from chemical industry with purine
After the aqueous phase mixing that serial sewage vacuum distillation is steamed, biochemical treatment is carried out into anaerobic digester and aerobic aeration pond；
Wherein, the volume ratio that wastewater from chemical industry produces serial sewage with purine is 8-12：1.
COD contents are mixed for the aqueous phase that 500-700mg/L wastewater from chemical industry is steamed with the serial sewage vacuum distillation of purine production
After conjunction, sodium dihydrogen phosphate is added, makes mixed liquor C:N:P mol ratio is 100:5:1.
The aqueous phase post processing distilled out is concretely comprised the following steps：COD contents 500-700mg/L wastewater from chemical industry enter homogeneous pond with
The aqueous phase distilled out adjusts pH after uniformly mixing, add and enter anaerobic digester after sodium dihydrogen phosphate, and obtained anaerobism muddy water is mixed
Enter aerobic activated sludge aeration tank after closing liquid regulation pH, aeration tank mixed liquor is back to anaerobic pond with 100-150% reflux ratios,
Aeration tank mixed liquor enters second pond and carries out mud-water separation, and sewage plant is sent in supernatant discharge, and precipitating sludge is back to aerobic aeration
Pond.
Anaerobic digester uses mechanical agitation mode under liquid to realize that muddy water is sufficiently mixed, and stopping waterpower in anaerobic digester stops
Hardly degraded organic substance after staying is largely converted into the small organic molecule of easily biological-degradable under acidification bacteria effect, then detests
Oxygen muddy water mixed solution enters aerobic activated sludge aeration tank.
The inlet flow-patterm of anaerobic digester is 6.0-9.0, preferably 7.0-8.0；Dissolved oxygen is 0.2-0.5mg/L, preferably 0.3-
0.4mg/L；Sludge concentration is 1.5-4.0g/L, preferably 2.0-3.0g/L；Hydraulic detention time is 60-100 hours, preferably 80-
90 hours.
The inlet flow-patterm of aerobic activated sludge aeration tank is 7.5-9.0, preferably 8.0-9.0；Dissolved oxygen is 3.0-7.0mg/L,
It is preferred that 4.0-6.0mg/L；Sludge concentration is 1.5-4.0g/L, preferably 2.0-3.0g/L；Hydraulic detention time is 40-60 hours,
It is preferred that 48-52 hours.After Aerobic biological process after hydraulic retention, majority of organic pollutants is degraded.
Aeration tank mixed liquor is partly refluxed to anaerobic pond, and water is diluted, and reduces organic pollution load variations pair
The impact of system simultaneously realizes denitrification denitrogenation.
The present invention first produces serial sewage to purine using air-distillation, vacuum distillation and pre-processed, the big portion steamed
Point aqueous phase with low concentration wastewater adjust water quality or with other chemical engineering sewage mixing biochemical treatments, final outflow water can reach sewage plant
Receiving requirement.
The present invention process object be high COD, high saliferous purine produced in series sewage, the sewage mix water COD and
NH3- N is up to 55000mg/L and more than 20000mg/L respectively, and with strong impulse smell, toxicity is big, it is difficult at biochemistry
Reason, using reoxidized after the direct oxidation of the advanced oxidation processes such as Fenton reagent or dilution be also difficult to be processed to it is up to standard.
After wastewater treatment of the present invention, COD≤500mg/L, NH3-N≤15mg/L。
Compared with prior art, the invention has the advantages that：
Economical rationality of the present invention, simple to operate, technical feasibility, it is easy to operate, wastewater toxicity can be effectively reduced, reduction is useless
Water COD, reduces NH3- N etc. content, finally makes water outlet can reach the receiving requirement of sewage plant.
Brief description of the drawings
Fig. 1, the present invention process flow diagram.
Embodiment
With reference to embodiment, the present invention is described further.
Embodiment 1
3 strands of sewage of purine production are with amination：Cyclization：Purine=0.7：1：1 ratio is mixed into the homogeneous pond of mixing and entered
Row homogeneous, the COD=56750mg/L of combined sewage, NH3- N=22032mg/L.Destilling tower is then pumped into, in theoretical cam curve 7
Destilling tower, steam under normal pressure 10% light component, the COD=205884mg/L of light component, NH3- N=29987mg/L.Steaming
During going out 10% light component, temperature is 89.5 DEG C when mixed liquor seethes with excitement, and bottom temperature is 97 DEG C during light component condensation discharging,
At the end of tower top temperature is 78 DEG C, the light component for steaming 10%, bottom temperature is 101.5 DEG C, and tower top temperature is 90 DEG C.Normal pressure steams
Treat that tower reactor is cooled to 68 DEG C after the light component for distillating 10%, then progress vacuum distillation goes out 60% under 0.06Mpa vacuum degree conditions
Moisture, vacuum distillation steams COD=947mg/L in aqueous phase, NH3- N=122mg/L.Raffinate COD=after distillation
91505mg/L, NH3- N=38897mg/L.Boiling temperature is 73 DEG C during vacuum distillation, and bottom temperature is when overhead condensation discharges
73 DEG C, tower top temperature is 68 DEG C, steams 79 DEG C of bottom temperature when 60% aqueous phase is completed, and tower top temperature is 69.5 DEG C.
COD contents enter homogeneous pond for 618mg/L chemical engineering sewage and produce what serial sewage vacuum distillation was steamed with purine
60% aqueous phase mixing, adjusts pH after uniform mixing, adds sodium dihydrogen phosphate, make mixed liquor C:N:P mol ratio is 100:5:1
Afterwards, into anaerobic digester, aerobic activated sludge aeration tank, aeration are entered after the anaerobism muddy water mixed solution regulation pH then obtained
Pond mixed liquor is back to anaerobic pond with 120% reflux ratio, and aeration tank mixed liquor enters second pond and carries out mud-water separation, supernatant
Sewage plant is sent in discharge, and precipitating sludge is back to aerobic aeration pond.
Wherein inlet flow-patterm=7.8 of anaerobic digester, dissolved oxygen 0.3mg/L, sludge concentration 2.5g/L, hydraulic detention time
88 hours.Inlet flow-patterm=8.9 of aerobic activated sludge aeration tank, dissolved oxygen 4.8mg/L, sludge concentration 3.0g/L, waterpower is stopped
Stay the time 50 hours.10% light component and vinasse steamed is burned.
COD contents produce serial sewage volume ratio 10 for 618mg/L chemical engineering sewage with purine：1.
Final process water outlet COD438.0mg/L, NH3-N13.0mg/L, have reached sewage plant requirement.
Embodiment 2
3 strands of sewage of purine production are with amination：Cyclization：Purine=0.7：1：1 ratio is mixed into the homogeneous pond of mixing and entered
Row homogeneous, the COD=59575mg/L of combined sewage, NH3- N=21125mg/L.Under the destilling tower of theoretical cam curve 8, normal pressure
Steam 10% light component, the COD=216000mg/L of light component, NH3- N=26550mg/L.Steaming 10% light component
During, temperature is 89 DEG C when mixed liquor seethes with excitement, and bottom temperature is 98 DEG C during light component condensation discharging, and tower top temperature is 77 DEG C,
At the end of the light component for steaming 10%, bottom temperature is 102 DEG C, and tower top temperature is 92 DEG C.Air-distillation goes out 10% light component
After treat that tower reactor is cooled to 67 DEG C, then carry out under 0.07Mpa vacuum degree conditions the moisture that vacuum distillation goes out 60%, vacuum distillation is steamed
Go out COD=880.8mg/L in aqueous phase, NH3- N=155.6mg/L.Raffinate COD=130350mg/L, NH after distillation3- N=
38425mg/L.Boiling temperature is 72 DEG C during vacuum distillation, and bottom temperature is 73 DEG C when overhead condensation discharges, and tower top temperature is 68
DEG C, 79 DEG C of bottom temperature when 60% aqueous phase is completed is steamed, tower top temperature is 69.5 DEG C.
COD contents enter homogeneous pond for 618mg/L chemical engineering sewage and produce what serial sewage vacuum distillation was steamed with purine
60% aqueous phase mixing, adjusts pH after uniform mixing, adds sodium dihydrogen phosphate, make mixed liquor C:N:P mol ratio is 100:5:1
Afterwards, into anaerobic digester, aerobic activated sludge aeration tank, aeration are entered after the anaerobism muddy water mixed solution regulation pH then obtained
Pond mixed liquor is back to anaerobic pond with 100% reflux ratio, and aeration tank mixed liquor enters second pond and carries out mud-water separation, supernatant
Sewage plant is sent in discharge, and precipitating sludge is back to aerobic aeration pond.
Wherein, inlet flow-patterm=7.6 of anaerobic digester, dissolved oxygen 0.4mg/L, sludge concentration 2.5g/L, during hydraulic retention
Between 85 hours.Inlet flow-patterm=8.6 of aerobic activated sludge aeration tank, dissolved oxygen 5.1mg/L, sludge concentration 2.8g/L, waterpower is stopped
Stay the time 50 hours.10% light component and vinasse steamed is sent into row burning disposal.
Chemical engineering sewage produces serial sewage volume ratio 9 with purine：1.
Final process water outlet COD422mg/L, NH3-N12.5mg/L, have reached the requirement that sewage plant receives.
Embodiment 3
3 strands of sewage of purine production are with amination：Cyclization：Purine=0.7：1：1 ratio is mixed into the homogeneous pond of mixing and entered
Row homogeneous, the COD=58750mg/L of combined sewage, NH3- N=22643mg/L.Destilling tower is then pumped into, in theoretical cam curve
Steamed under 10 destilling tower, normal pressure 11% light component, the COD=215384mg/L of light component, NH3- N=29387mg/L.
During steaming 11% light component, temperature is 89 DEG C when mixed liquor seethes with excitement, and bottom temperature is 96 DEG C during light component condensation discharging,
At the end of tower top temperature is 77 DEG C, the light component for steaming 11%, bottom temperature is 101 DEG C, and tower top temperature is 95 DEG C.Air-distillation
Treat that tower reactor is cooled to 69 DEG C after the light component for going out 11%, then progress vacuum distillation goes out 58% under 0.06Mpa vacuum degree conditions
Moisture, vacuum distillation steams COD=967mg/L in aqueous phase, NH3- N=162mg/L.Raffinate COD=91723mg/ after distillation
L, NH3- N=38639mg/L.Boiling temperature is 73 DEG C during vacuum distillation, and bottom temperature is 73 DEG C, tower top when overhead condensation discharges
Temperature is 68 DEG C, steams 79 DEG C of bottom temperature when 58% aqueous phase is completed, and tower top temperature is 69.5 DEG C.
COD contents enter homogeneous pond for 700mg/L chemical engineering sewage and produce what serial sewage vacuum distillation was steamed with purine
58% aqueous phase mixing, adjusts pH after uniform mixing, adds sodium dihydrogen phosphate, make mixed liquor C:N:P mol ratio is 100:5:1
Afterwards, into anaerobic digester, aerobic activated sludge aeration tank, aeration are entered after the anaerobism muddy water mixed solution regulation pH then obtained
Pond mixed liquor is back to anaerobic pond with 150% reflux ratio, and aeration tank mixed liquor enters second pond and carries out mud-water separation, supernatant
Sewage plant is sent in discharge, and precipitating sludge is back to aerobic aeration pond.
Inlet flow-patterm=7.9 of anaerobic digester, dissolved oxygen 0.35mg/L, sludge concentration 2.8g/L, hydraulic detention time 85
Hour, inlet flow-patterm=8.8 of aerobic activated sludge aeration tank, dissolved oxygen 5.1mg/L, sludge concentration 3.0g/L, during hydraulic retention
Between 50 hours.10% light component and vinasse steamed carries out burning disposal.
Chemical engineering sewage produces serial sewage volume ratio 8 with purine：1.
Final process water outlet COD413mg/L, NH3- N11.3mg/L, has reached the requirement that sewage plant receives.
Embodiment 4
3 strands of sewage of purine production are with amination：Cyclization：Purine=0.7：1：1 ratio is mixed into the homogeneous pond of mixing and entered
Row homogeneous, the COD=58550mg/L of combined sewage, NH3- N=22463mg/L.Destilling tower is then pumped into, in theoretical cam curve
Steamed under 10 destilling tower, normal pressure 9% light component, the COD=213334mg/L of light component, NH3- N=29486mg/L.
During steaming 9% light component, temperature is 89.5 DEG C when mixed liquor seethes with excitement, and bottom temperature is 97 during light component condensation discharging
DEG C, at the end of tower top temperature is 78 DEG C, the light component for steaming 9%, bottom temperature is 101.5 DEG C, and tower top temperature is 90 DEG C.Normal pressure
Treat that tower reactor is cooled to 70 DEG C after the light component for distilling out 9%, then progress vacuum distillation goes out 62% under 0.06Mpa vacuum degree conditions
Moisture, vacuum distillation steams COD=967mg/L in aqueous phase, NH3- N=162mg/L.Raffinate COD=after distillation
91723mg/L, NH3- N=38639mg/L.Boiling temperature is 73 DEG C during vacuum distillation, and bottom temperature is when overhead condensation discharges
73 DEG C, tower top temperature is 68 DEG C, steams 79 DEG C of bottom temperature when 62% aqueous phase is completed, and tower top temperature is 69.5 DEG C.
COD contents enter homogeneous pond for 550mg/L chemical engineering sewage and produce what serial sewage vacuum distillation was steamed with purine
62% aqueous phase mixing, adjusts pH after uniform mixing, adds sodium dihydrogen phosphate, make mixed liquor C:N:P mol ratio is 100:5:1
Afterwards, into anaerobic digester, aerobic activated sludge aeration tank, aeration are entered after the anaerobism muddy water mixed solution regulation pH then obtained
Pond mixed liquor is back to anaerobic pond with 150% reflux ratio, and aeration tank mixed liquor enters second pond and carries out mud-water separation, supernatant
Sewage plant is sent in discharge, and precipitating sludge is back to aerobic aeration pond.
Inlet flow-patterm=7.7 of anaerobic digester, dissolved oxygen 0.30mg/L, sludge concentration 3.0g/L, hydraulic detention time 88
Hour.The main technologic parameters of aerobic activated sludge aeration tank are pH8.9, dissolved oxygen 4.9mg/L, sludge concentration 3.3g/L, water
51 hours power residence times.Final process water outlet COD397mg/L, NH3- N10.8mg/L, has reached that chemical industrial park sewage plant connects
The requirement received.
Chemical engineering sewage produces serial sewage volume ratio 12 with purine：1.
10% light component and vinasse steamed carries out burning disposal.
Final process water outlet COD423mg/L, NH3- N12.1mg/L, has reached the requirement that sewage plant receives.
Comparative example 1
3 strands of sewage of purine production are with amination：Cyclization：Purine=0.7：1：1 ratio mixing, the COD=of combined sewage
56750mg/L, NH3- N=22032mg/L.Steamed under the destilling tower of theoretical cam curve 7, normal pressure 10% light component, light group
The COD=205884mg/L, NH divided3- N=29987mg/L.With the identical purine combined sewage of embodiment 1, in same process condition
Under, air-distillation goes out COD44250mg/L, BOD in 10% light component, remaining 90% raffinate53990mg/L, BOD5/ COD is only
0.09, still fall within not biochemical sewage.Iron-carbon micro-electrolysis processing experiment is carried out to 90% raffinate, first by the pH of raffinate
3.0 are adjusted to by 7.10, and iron carbon dosing ratio 50% measures COD39000mg/L after aerating oxidation time 2 h, COD clearances are only
11.8%.Further increase iron carbon dosing ratio, the extension aerating oxidation time can not improve COD clearances.
Comparative example 2
Fenton reagent oxidation is carried out except COD experiments for 204800mg/L purine process spent water to COD contents, first by purine
5 times of dilution of sewage, then pH is adjusted to 3, a certain amount of ferrous sulfate is added, 5% (v/v) Fenton reagent H is then added2O2, stirring
Oxidation 3 hours, is settled 0.5 hour, and supernatant adjusts back pH to more than 7.0 post analysis COD contents, and as a result COD is before oxidation processes
40960mg/L (dilution 5 times after) fall below 18750mg/L, clearance 54.2%.Continue to improve Fenton reagent dosage, prolong
COD clearances can not be significantly increased in long stirring oxidization time.
Result of the test shows, steams after 10% light component (the mainly small organic molecule of irritant smell), remaining
90% purine vinasse COD is still very high, and the upper limit of detection beyond BOD analyzers is, it is necessary to dilute.It will be distilled with distilled water
Raffinate is diluted after 80 times, salt content and the virose pollutant concentration of biology tool is all greatly lowered in water, explanation is steamed
After 10% light component, remaining 90% purine sewage is still difficult to biochemistry.Steam after 10% light component, then steam 70% aqueous phase, should
Steam water biodegradability good, illustrate most of poisonous, hard-degraded substance in light component and residual solution.Therefore, the present invention is adopted
First serial sewage is produced to purine with rectifying, vacuum distillation to pre-process, the most aqueous phase steamed is useless with low concentration again
Biochemical treatment is carried out after water adjustment water quality, final outflow water reaches the requirement that sewage plant receives.
Claims (7)
1. a kind of purine produces the processing method of waste water, it is characterised in that the amination that is produced in purine production process, cyclization, fast
After the mixing of three strands of sewage of purine, carry out air-distillation, distill out light component, after air-distillation after tower reactor is cooled to 67-70 DEG C
Vacuum distillation under vacuum condition, steams aqueous phase, and raffinate discharge distillation still is burned after being mixed with the light component steamed, steams aqueous phase and enter
Row post processing；
Air-distillation steams the ratio 6%-12% of light component；Vacuum distillation vacuum 0.05-0.08 Mpa；Steam watr-proportion
50%-70%；
During air-distillation, temperature is 88-90 DEG C when mixed liquor seethes with excitement；During light component condensation discharging, bottom temperature is 96-98
DEG C, tower top temperature is 76-78 DEG C；At the end of steaming light component, bottom temperature is 101-103 DEG C, and tower top temperature is 90-100 DEG C；
Boiling temperature is 71-73 DEG C during vacuum distillation, when overhead condensation discharges, and bottom temperature is 73 DEG C, and tower top temperature is 68 DEG C；
When steaming aqueous phase completion, bottom temperature is 79 DEG C, and tower top temperature is 69.5 DEG C.
2. purine according to claim 1 produces the processing method of waste water, it is characterised in that the destilling tower tower that distillation is used
Plate number is 4-10 blocks.
3. purine according to claim 1 produces the processing method of waste water, it is characterised in that after the aqueous phase that vacuum distillation goes out
Process step is：COD contents produce the aqueous phase that serial sewage vacuum distillation is steamed for 500-700mg/L wastewater from chemical industry with purine
After mixing, biochemical treatment is carried out into anaerobic digester and aerobic aeration pond；
Wherein, the volume ratio that wastewater from chemical industry produces serial sewage with purine is 8-12：1.
4. purine according to claim 3 produces the processing method of waste water, it is characterised in that COD contents are 500-
After 700mg/L wastewater from chemical industry is mixed with the aqueous phase that the serial sewage vacuum distillation of purine production is steamed, sodium dihydrogen phosphate is added, is made
Mixed liquor C:N:P mol ratio is 100:5:1.
5. purine according to claim 3 produces the processing method of waste water, it is characterised in that the inlet flow-patterm of anaerobic digester
For 6.0-9.0；Dissolved oxygen is 0.2-0.5mg/L；Sludge concentration is 1.5-4.0g/L；Hydraulic detention time 60-100 hours.
6. purine according to claim 3 produces the processing method of waste water, it is characterised in that aerobic activated sludge aeration tank
Water inlet be pH7.5-9.0；Dissolved oxygen 3.0-7.0mg/L；Sludge concentration 1.5-4.0g/L；Hydraulic detention time 40-60 hours.
7. purine according to claim 3 produces the processing method of waste water, it is characterised in that after the aqueous phase that vacuum distillation goes out
Process step is：COD contents 500-700mg/L wastewater from chemical industry, which enters after aqueous phase of the homogeneous pond with distilling out uniformly is mixed, to be adjusted
PH, adds and enters anaerobic digester after sodium dihydrogen phosphate, and it is dirty to enter aerobic activity after obtained anaerobism muddy water mixed solution regulation pH
Mud aeration tank, aeration tank mixed liquor is back to anaerobic pond with 100-150% reflux ratios, and aeration tank mixed liquor is carried out into second pond
Sewage plant is sent in mud-water separation, supernatant discharge, and precipitating sludge is back to aerobic aeration pond.
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