CN109851161A - Produce the processing method of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde - Google Patents
Produce the processing method of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde Download PDFInfo
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- CN109851161A CN109851161A CN201910044366.1A CN201910044366A CN109851161A CN 109851161 A CN109851161 A CN 109851161A CN 201910044366 A CN201910044366 A CN 201910044366A CN 109851161 A CN109851161 A CN 109851161A
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- benzyl dichloride
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Abstract
The invention discloses production biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde processing method, comprising the following steps: neutralize be centrifuged, except formaldehyde, MVR evaporation, UASB Anaerobic Treatment, hydrolysis acidification pool, catalytic oxidation, sedimentation in secondary sedimentation tank, two-stage flocculation sedimentation, ozone oxidation, biofilter Air Exposure, disappear ammonia spirit processing and Treatment of Sludge.Compared with prior art, the beneficial effects of the present invention are: with minimum operating cost, and best solution, reach evaporation separating effect, so that production cost is reduced, after advanced treating transformation, waste water COD concentration of emission drops to 200mg/L from 500mg/L, ammonia nitrogen concentration of emission drops to 25mg/L from 40mg/L, takes charge of Wastewater Pollutant emission matching standard, and qualified discharge.
Description
Technical field
The invention belongs to sewage treatment field, it is related to producing the place of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde
Reason method.
Background technique
Certain chemical science and technology company originally had fluorescent whitening agent production line, rear to increase biphenyl-benzyl dichloride production line and adjacent sulphur again
Sour sodium benzaldehyde production line.
As shown in Figure 1, existing sewage treatment process is: fluorescent whitening agent waste water sequentially enters comprehensive adjustment pond and neutralization
Through plate and frame filter press filters pressing after the processing of pond, sludge enters sludge concentration tank, and filtrate sequentially enters hydrolysis acidification pool, catalytic oxidation
After pond, secondary settling tank and two-stage flocculation sedimentation tank, qualified discharge pond is finally entered, is generated in secondary settling tank and two-stage flocculation sedimentation tank
Sludge also enters sludge concentration tank, and for sludge concentration tank after filter press filters pressing, supernatant enters comprehensive adjustment pond, and sludge is transported outward,
The outer processing of committee.
But produce the waste water that brightening agent, ortho-sulfonic acid sodium benzaldehyde, biphenyl-benzyl dichloride generate and belong to high-salt wastewater, it is existing
Sewage disposal system main body uses " hydrolysis acidification+catalytic oxidation+two-stage flocculation sedimentation " technique, because needing in wastewater treatment process
Salt is removed, and newly increases benzyl dichloride waste water in wastewater treatment process, a large amount of zinc mud, salt and first are contained in waste water
Aldehyde, existing triple effect evaporation processing energy consumption is high, processing capacity is insufficient, poses a big pressure to entire waste water treatment system, Yi Zao
It can not operate normally at system；In addition, existing sewerage is without removal formaldehyde；Waste water molecular weight is big, difficult to degrade after pretreatment；
And the discharge of wastewater adapter tube standard of original garden is COD < 500mg/L, ammonia nitrogen < 40mg/L, and new garden waste water adapter tube standard
It is changed to COD < 200mg/L, ammonia nitrogen < 25mg/L, for this purpose, the chemical company is badly in need of carrying out upgrading to existing sewage disposal system changing
It makes.
Summary of the invention
The problem to be solved by the invention is as follows in view of the above shortcomings of the prior art, and production biphenyl-benzyl dichloride is provided
And the processing method of the produced sewage of ortho-sulfonic acid sodium benzaldehyde.
In order to solve the above technical problems, the technical solution adopted by the present invention is that:
The processing method of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde is produced, following steps:
(1) the fluorescer waste water that the benzyl dichloride waste water and production fluorescer generated first to production biphenyl-benzyl dichloride generates
Neutralization reaction is carried out, ph=7 is made, the benzyl dichloride waste water after neutralization is centrifuged using centrifuge, removes zinc-containing sludge therein；
(2) benzyl dichloride waste water and fluorescer waste water after removing zinc mud enter oxidation of formaldehyde device and are aoxidized, and are aoxidizing
It is 1%-3% hydrogen peroxide that concentration is added in the process, removes formaldehyde and salts substances in waste water, and benzyl dichloride is useless after being pre-processed
Water and fluorescer waste water, the sludge that oxidation of formaldehyde process generates enter sludge concentration tank；
(3) waste water of benzyl dichloride waste water and fluorescer waste water after the evaporation of MVR falling film evaporator enters homogenizing after pre-processing
Pond produces ortho-sulfonic acid sodium benzaldehyde and waste water after the evaporation of MVR forcing vaporiser of the sulfonic acid aldehyde waste water that generates, workshop appliance punching
Waste water, which enters in balancing reservoir, after wash water, sanitary sewage and flocculation sedimentation is mixed, and composite waste is obtained；
(4) composite waste enters upflow anaerobic sludge blanket reactor UASB progress anaerobic reaction, removes in composite waste
Organic matter；
(5) composite waste after UASB Anaerobic Treatment sequentially enters hydrolysis acidification pool and contact-oxidation pool, and acid is hydrolyzed
Change and catalytic oxidation is handled, further removes the organic matter in composite waste；
(6) treated that composite waste is introduced into secondary settling tank is precipitated for catalytic oxidation, then to sequentially enter level-one flocculation heavy
Shallow lake pond and second level flocculation sedimentation tank carry out two-stage flocculation sedimentation, remove wherein insoluble substance, the sludge generated in secondary settling tank
Enter sludge concentration tank with the sludge generated in two-stage flocculation sedimentation tank；
(7) composite waste after flocculation sedimentation enters ozone oxidation pond progress oxidation processes；
(8) composite waste after ozone oxidation enters biological aerated filter and carries out aeration degrading waste water COD, passes through aeration life
Whether the experiment of object filter tank, examine COD up to standard, discharge after COD is up to standard；
(9) supernatant of sludge concentration tank enters step the balancing reservoir in (3), and the sludge in sludge concentration tank is through sheet frame pressure
The sludge outward transport generated after filter compression, outer processing of entrusting.
Benzyl dichloride waste water is transferred to PH to 3 by the liquid alkaline for being first 30-40% with concentration in step (1), then is adjusted and given up with soda ash
Water pH to 7.
In step (3), waste water, workshop appliance flushing water, life of the p-sulfonic acid aldehyde waste water after the evaporation of MVR forcing vaporiser
Waste water carries out homogenization after sewage and flocculation sedimentation.
In step (7), the gas production of the ozone generator in ozone oxidation pond is 3kg/h.
A set of ammonia spirit chemicals dosing plant that disappears is set after the biological aerated filter in step (8), removes the ammonia nitrogen in waste water.
The evaporation rate of MVR falling film evaporator is 6.8t/h, and the evaporation rate of MVR forcing vaporiser is 3.0t/h.
In step (3), the evaporating temperature of MVR forcing vaporiser is set as 85 DEG C, after secondary steam is compressed, and temperature can increase
To 90-95 DEG C.
Compared with prior art, the beneficial effects of the present invention are: with minimum operating cost and best solution party
Case, to reach evaporation separating effect, to reduce production cost, waste water is through " MVR falling liquid film (6.8t/h)+MVR forces (3.0t/h)
+ UASB+ hydrolysis acidification+catalytic oxidation+second level flocculation sedimentation+ozone generator (3kg/h)+biological aerated filter+disappear ammonia spirit dress
Set ", after advanced treating transformation, waste water COD concentration of emission drops to 200mg/L from 500mg/L, and ammonia nitrogen concentration of emission is dropped from 40mg/L
To 25mg/L, Wastewater Pollutant emission matching standard, and qualified discharge.
MVR falling film evaporator and MVR forcing vaporiser thoroughly solve deficiency existing for triple effect evaporation, enhance high-salt wastewater
Pretreatment potentiality alleviates system wastewater treatment pressure.
Oxidation of formaldehyde device destroys formaldehyde in waste water under the high temperature conditions, enhances hc effluent pretreatment potentiality, after reduction
Continuous biochemical system handles load.
The UASB anaerobism equipment high-COD waste water big, difficult to degrade for molecular weight, further degrade COD, alleviates biochemical treatment
Pressure.
Ozone generator, disappear ammonia spirit device, and COD, ammonia nitrogen is effectively reduced, and water outlet meets new adapter tube standard.If garden
Sewage adapter tube standard COD < 500mg/L, ammonia nitrogen < 25mg/L, ozone oxidation system are out of service.
Detailed description of the invention
Fig. 1 is the flow diagram of the existing sewage treatment process in the chemical plant；
Fig. 2 is that the process of the processing method of production biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde of the invention is shown
It is intended to.
Specific embodiment
Presently in connection with embodiment and attached drawing, the present invention is described in further detail.Attached drawing is simplified schematic diagram,
The basic structure of the invention will be illustrated schematically only, therefore it only shows the composition relevant to the invention.
As shown in Fig. 2, the processing method of production biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde, following steps:
(1) the fluorescer waste water that the benzyl dichloride waste water and production fluorescer generated first to production biphenyl-benzyl dichloride generates
Neutralization reaction is carried out, benzyl dichloride waste water is transferred to PH to 3 by the liquid alkaline for being first 30-40% with concentration, then adjusts wastewater pH with soda ash
To 7, the benzyl dichloride waste water after neutralization is centrifuged using centrifuge, removes zinc-containing sludge therein；
(2) benzyl dichloride waste water and fluorescer waste water after removing zinc mud enter oxidation of formaldehyde device and are aoxidized, and are aoxidizing
It is 1%-3% hydrogen peroxide that concentration is added in the process, removes formaldehyde and salts substances in waste water, and benzyl dichloride is useless after being pre-processed
Water and fluorescer waste water, the sludge that oxidation of formaldehyde process generates enter sludge concentration tank；
(3) waste water of benzyl dichloride waste water and fluorescer waste water after the evaporation of MVR falling film evaporator enters homogenizing after pre-processing
Pond produces ortho-sulfonic acid sodium benzaldehyde and waste water after the evaporation of MVR forcing vaporiser of the sulfonic acid aldehyde waste water that generates, workshop appliance punching
Waste water, which enters in balancing reservoir, after wash water, sanitary sewage and flocculation sedimentation is mixed, and the evaporation rate of MVR falling film evaporator is
The evaporating temperature of 6.8t/h, MVR forcing vaporiser is set as 85 DEG C, after secondary steam is compressed, and temperature can be increased to 90-95 DEG C,
The evaporation rate of MVR forcing vaporiser be 3.0t/h, p-sulfonic acid aldehyde waste water through MVR forcing vaporiser evaporation after waste water, workshop
Waste water carries out homogenization after equipment flushing water, sanitary sewage and flocculation sedimentation, obtains composite waste；
(4) composite waste enters upflow anaerobic sludge blanket reactor UASB progress anaerobic reaction, removes in composite waste
Organic matter,
(5) composite waste after UASB Anaerobic Treatment sequentially enters hydrolysis acidification pool and contact-oxidation pool, and acid is hydrolyzed
Change and catalytic oxidation is handled, further removes the organic matter in composite waste；
(6) treated that composite waste is introduced into secondary settling tank is precipitated for catalytic oxidation, then to sequentially enter level-one flocculation heavy
Shallow lake pond and second level flocculation sedimentation tank carry out two-stage flocculation sedimentation, remove wherein insoluble substance, the sludge generated in secondary settling tank
Enter sludge concentration tank with the sludge generated in two-stage flocculation sedimentation tank；
(7) composite waste after flocculation sedimentation enters ozone oxidation pond progress oxidation processes, the ozone in ozone oxidation pond
The gas production of generator is 3kg/h；
(8) composite waste after ozone oxidation enters biological aerated filter and carries out aeration degrading waste water COD, passes through aeration life
Whether the experiment of object filter tank, examine COD up to standard, discharge after COD is up to standard；A set of ammonia spirit dosing dress that disappears is set after biological aerated filter
It sets, removes the ammonia nitrogen in waste water；The ammonia miraculous cure agent that disappears can ensure discharged wastewater met the national standard in a short time, therefore work as biological aerated filter
Water outlet ammonia nitrogen is directly added into the ammonia spirit that disappears when 25mg/L is not achieved, and when the standard water discharge of filter tank, the ammonia miraculous cure agent that disappears is just as emergency medicament
It uses；
(9) supernatant of sludge concentration tank enters step the balancing reservoir in (3), and the sludge in sludge concentration tank is through sheet frame pressure
The sludge outward transport generated after filter compression, outer processing of entrusting.
Embodiment 1
Waste portion is determined after detecting to the water sample (Workshop Production waste water is after being evaporated under reduced pressure) that the chemical company provides
Point index is as follows:
The former water quality indicator list of table 1.1
Effluent index is the water quality indicator for being emitted into municipal sewage plant that local environmental protection administration requires, and is detailed in following table:
1.2 effluent quality index list of table
| COD(mg/L) | NH3-N(mg/L) | pH | Total salt (mg/L) | Total phosphorus (mg/L) |
| ≤500 | ≤40 | 6~8 | ≤5000 | ≤1.0 |
Wastewater treatment experimentation and data
(1) it neutralizes centrifugation: neutralization experiment being carried out to waste water using liquid alkaline, is first that 30-40% liquid alkaline is transferred to PH extremely with concentration
3, then wastewater pH is adjusted to 7 with soda ash, then benzyl dichloride waste water is filtered, the effect phase of the effect more centrifugal filtration of suction filtration
Together.Take the content of COD and formaldehyde in supernatant detection waste water.
(2) it evaporates: processing is evaporated to supernatant.Under the conditions of pH is 7, then it is added in waste water, 2%, 3%
Hydrogen peroxide is evaporated experiment respectively, COD, content of formaldehyde in its waste water of effluent monitoring after evaporation.
2 hours first are kept the temperature at 70 degrees Celsius, detection data is as follows:
| Water sample | Formolite number | Formaldehyde removal rate | COD value | COD removal rate |
| Waste water after neutralization | 12678 | 15530 | ||
| After 2% dioxygen water evaporation | 2307 | 81.8% | ||
| After 3% dioxygen water evaporation | 326 | 97.5% | 4369 | 71.8% |
| Sewage plant collection water sample | 124.2 | 3333.5 | ||
| After the evaporation of sewage plant collection water sample | 122.3 | 1.5% | 1674.5 | 49.8% |
After being evaporated respectively using 2% and 3% hydrogen peroxide to waste water after neutralization, the ammonia nitrogen removal of 3% hydrogen peroxide is found
Rate is more much higher than 2%, and the water sample evaporated using 3% hydrogen peroxide can directly carry out experimental anaerobic from index.
(3) experimental anaerobic: the granule sludge of 500mL will be added in 1L volumetric flask, and water sample will be added in volumetric flask to appearance
Until measuring bottle is full.By the benzyl dichloride waste water water sample after 3% dioxygen water evaporation with water sample of the sulfonic acid aldehyde waste water after evaporating by 1:1
Mixing and the water sample after 3% dioxygen water evaporation carry out one group of experimental anaerobic respectively.The variation feelings of monitoring waste water COD and PH daily
Condition is added liquid alkaline in volumetric flask and recalls to pH to 7-8 when wastewater pH is lower than 7.Volumetric flask needs to shake daily 3 times, every time
Shaking needs uniformly to mix sludge in waste water and waste water.
Waste water index see the table below after fermentation in 48 hours:
Experimental result can be seen that Anaerobic Treatment will not remove ammonia nitrogen value, and ammonia nitrogen value is higher will affect anaerobic bacteria
To the removal rate of COD value, is reacted in first 24 hours since observing anaerobism in experimentation relatively acutely, generate methane gas
Steep more, reaction rate tends to be steady as time went on.
(4) by simulating existing sewage plant technique, and acidification is hydrolyzed using the sludge of anoxic pond, uses aerobic tank
Sludge carries out Aerobic Process for Treatment, carries out flocculation sedimentation using PAC, PAM, the ammonia nitrogen value and COD value situation for obtaining water sample are as follows:
| Water sample | Ammonia nitrogen value | Ammonia nitrogen removal frank | COD value | COD removal rate |
| After 3% dioxygen water evaporation water anaerobism | 330.5 | 1901.5 | ||
| After hydrolysis acidification | 210.8 | 36.2% | 1391.5 | 26.8% |
| After Aerobic Process for Treatment | 41.3 | 80.4% | 1084.0 | 22.1% |
| After flocculation sedimentation | 28.9 | 30.0% | 339.8 | 68.7% |
It can be seen that the data result obtained by simulated experiment by upper table data to approach with the ratio of prediction, finally
The ammonia nitrogen value and COD value of water outlet can reach discharge standard.
Embodiment 2
The water and water quality of the various waste water in the chemical plant
2.1 benzyl dichloride waste water of table, sulfonic acid aldehyde waste water quality water
Other waste water quality waters of table 2.2
Waste water characteristic contamination factors check
| Name of product | Waste water characterization factor |
| Ortho-sulfonic acid sodium benzaldehyde | COD, SS, total salt |
| Biphenyl-benzyl dichloride | COD, formaldehyde, toluene, total zinc, total phosphorus |
Local emission request
It is required according to local environmental protection administration, discharge of wastewater index is to be emitted into the water quality indicator of garden sewage treatment plant, tool
Body is as follows:
Waste water treatment step is as follows:
Step 1: neutralizing centrifugation
Neutralization reaction is carried out to the benzyl dichloride waste water and fluorescer waste water that enter in sewage plant collecting-tank, makes ph=7, neutralizes
Benzyl dichloride waste water afterwards is centrifuged using centrifuge, removes zinc-containing sludge therein, the waste water after centrifugation enters wastewater collection pond.
Step 2: oxidation of formaldehyde
Waste water in wastewater collection pond enters oxidation of formaldehyde device and is aoxidized, and it is 3% that concentration is added in oxidation process
Hydrogen peroxide removes formaldehyde and salts substances in waste water, benzyl dichloride waste water and fluorescer waste water, oxidation of formaldehyde after being pre-processed
The sludge that process generates enters sludge concentration tank.
Step 3: MVR processing technological flow
Benzyl dichloride waste water and fluorescer waste water enter MVR falling film evaporator and are evaporated after pretreatment, and sulfonic acid aldehyde waste water is equal
It is evaporated into MVR forcing vaporiser.
The objective of this programme is: with minimum operating cost and best solution, imitating to reach evaporation separation
Fruit, to reduce production cost.
MVR process introduction is as follows:
The variation of the solubility with temperature of solute is less within the scope of evaporating temperature and material boiling point liter is higher.Scheme rank
Section is risen using the highest solution boiling point of normal pressure saturated mode boiling point as theoretical basis.Value is that material saturated sodium-chloride is molten in the program
Liquid boiling point rises about 10 DEG C of terminal, and ammonium chloride solution boiling point rises about 15 DEG C of terminal.
MVR-FC continuous crystallizing system is handled, and MVR system couples FC crystallizer, and system selects mixed-flow pump, biggish
Flow velocity can also reduce fouling tendency, extend the cleaning frequency.And mixed-flow pump has larger and suitable flow, and this is also control object
The necessary condition for expecting crystallizing metastable zone, creates condition to grow the crystal of suitable scale.
Vapour compression machine select separate unit positive displacement compressor, when fluid is from heat exchanger into vapour-liquid crystallizer, using center into
The mode of material.Since supplied materials does not have thermal sensitivity, optional evaporating temperature is any, and it is 85 DEG C that design, which is fixed tentatively,.Higher centrifugation temperature
Degree can make material water capacity reduce thus this case selection high temperature centrifugation, 85 DEG C of centrifuging temperature.
MVR evaporator basic procedure feed liquid process
The feed liquid device preheated first for adjusting PH to 7 recycles condensate liquid sensible heat, is pumped into following for circulation heat exchanger by raw material
Endless tube enters separator after circulation pipe heats up and evaporates, and solution flashes at two-phase interface, and solution is immediately in circulating pump after evaporation
Attraction under flow downward to be mixed into fresh feed liquid and recycle next time, discharging to be achieved discharges after requiring.
Steam flow
Secondary steam in multi-cycle separation device is moved upwards into roots-type vapour compression machine, and roots-type vapour compression machine will
Secondary steam is compressed to the shell side release latent heat of return circulation heat exchanger after technological design temperature, and condensed water enters condensate liquid collection
Tank.
Crystallizer/separator
Feed liquid enters crystallizer/separator evaporation after circulation heat exchanger heat temperature raising, and evaporation process is in totally-enclosed shape
It is carried out continuously under state, temperature, pressure and feed concentration are positively retained at the state for being most appropriate to evaporation in equipment.Crystallizer/point
From efficient mist eliminator is equipped with inside device, vapor-liquid separation efficiency can be improved, reduce entrainment.
Crystallizer/separator interior is equipped with spray equipment, and there are two effects, first is that mist eliminator is washed, second is that avoiding object
Expect wall built-up.
Circulation heat exchanger
Using tube-sheet heat exchanger.It is both material heater due to the effect of MVR, while is also the condensation of secondary steam
Device.With the features such as heat transfer efficiency height, occupied area is small, and equipment price is low.
Partial organic substances can gradually be stained in heat transfer tube wall and cause convective heat-transfer coefficient in pipe during evaporation
Decline, causes K value to decline to a great extent, easy-to-dismount to use heat exchanger convenient for this secondary design of cleaning in operational process from now on
Short tube, convenient for maintenance from now on.
Heater tube side material selection Ta2, shell side material selection 316L.
Vapour compression machine
Using all steel vapour compression machine designed exclusively for both vapor compression, have noise small, shakes small, high reliablity
The advantages that.
Flow-interpret
Feed liquid to be processed squeezes into vapo(u)rization system by pumping.Feed liquid squeezes into tube-sheet heat exchanger by feed pump, changes in tube-sheet type
Feeding liquid carries out heat exchange with steam condensate (SC) in evaporator in hot device, after feeding liquid preheating, into crystallizer/separator progress
Evaporation.
The secondary steam come out from crystallizer/separator, into MVR compressibility.After secondary steam is compressed, temperature can
91 DEG C or so are increased to, compressed steam enters back into circulation heat exchanger heated material.During heated material, this part is steamed
Vapour is condensed into water and is discharged by water pump, and temperature is about 91 DEG C, and circulation heat exchanger had not only been used as heater but also the conduct of material at this time
The cooler of steam after pressure.
Secondary steam after material after preheating enters circulation heat exchanger, and after compression after temperature rise exchanges heat, entire to be
System reaches thermal balance, does not need external fresh steam at this time and is heated, it is only necessary to which compressor is flat to maintain the heat of whole system
Weighing apparatus.
Step 4: benzyl dichloride waste water and fluorescer waste water are useless after the evaporation of MVR falling film evaporator after balancing reservoir pretreatment
Water enters balancing reservoir, produce ortho-sulfonic acid sodium benzaldehyde and waste water after the evaporation of MVR forcing vaporiser of the sulfonic acid aldehyde waste water that generates,
Waste water, which enters in balancing reservoir, after workshop appliance flushing water, sanitary sewage and flocculation sedimentation is mixed, and composite waste is obtained, to mixed
It closes waste water and carries out homogenization.
Step 5: biochemical treatment process
The Anaerobic Treatment of composite waste is handled using Up-flow Anaerobic Sludge Bed (UASB).
Up-flow Anaerobic Sludge Bed (UASB) technology at home and abroad has been developed as the mainstream technology of Anaerobic Treatment
One of, there is no carrier in UASB, sewage is from bottom even into flowing up, granule sludge (sludge wadding body) is in rising
Suspended state is under water flow and bubble.Reactor lower part is the higher Sludge Bed of concentration, and top is that concentration is lower outstanding
Floating sludge blanket, organic matter are converted into methane and carbon dioxide gas herein.There is three phase separator on the top of reactor, can take off
Gas and return to sludge settling in reactor.The COD load of UASB is higher, and sludge concentration is up to 100-150g/L in reactor,
Therefore COD removal efficiency is more three times higher than common anaerobic reactor, up to 80%~95%.Its start time it is short, can be interrupted or
Seasonality operation, investment is low, and operational management is simple.
Step 6: anerobic sowage and Aerobic
Composite waste after UASB Anaerobic Treatment sequentially enters hydrolysis acidification pool and contact-oxidation pool, be hydrolyzed acidification and
Catalytic oxidation processing further removes the organic matter in composite waste
Sewage is handled using anaerobic-aerobic A/O method, and since waste water contains, organic matter is higher, simple aerobe
Processing is difficult to reach requirement, in addition, sludge treatment problem is also a great problem that field of waste water treatment is not resolved, therefore,
In order to seek efficient low-consume, New Wastewater Treatment Technique with low investment, the in recent years combination in anaerobism and aerobic process, aerobic process
Strengthen two aspects and does a large amount of research, the progress of making a breakthrough property.
The hydrolysis and acidification stage of anaerobic-aerobic A/O method technology utilization Anaerobic Treatment, and abandon methane phase (alkalinity hair
Ferment) stage, the main purpose of Anaerobic Treatment is to realize the conversion of refractory organic with non-hydrolytic effect by hydrolyzing, and is led to
It crosses molecular structure and changes (open loop, scission of link, cracking, group replace, reduction etc.), the organic matter point for the difficult for biological degradation that makes that structure is complicated
Son is converted to can at a slow speed or the organic matter of fast degraded biologically, to be obviously improved the bio-treatment Feasibility and decoloration effect of sewage
Fruit, making final electron acceptor includes refractory organic (group or chemical bond in molecular structure).Keep effluent quality steady
It is fixed, impact load is reduced, creates conditions for Aerobic Process for Treatment, using this process, preferably solves the problems, such as SS (suspended matter).It is another
The characteristics of aspect is that the excess sludge that aerobic section generates all flows back into anaerobism section, since anaerobism section has sufficiently long biosolids
Residence time (SRT), sludge can carry out thorough anaerobic digestion in anaerobism section, to keep excess sludge whole in cyclic process
It is decomposed into H2O and CO2, whole system reaches the sludge balance of itself, and it is dirty to efficiently solve pulp waste water for few row or not blowdown mud
The problem of mud, while biological denitrificaion can also be played the role of.Therefore process anaerobism section have double action, first is that waste water into
Row pretreatment, improves its biochemical, and adsorb, a part of organic matter of degrading；Second is that the sludge to system carries out digestion process.
1, the feature of process aspect:
(1) A/O mostly uses the biologic packing material that large specific surface area, voidage are high, water flow is unobstructed, and plus sufficient organic matter
And dissolved oxygen, inhabit proliferation suitable for microorganism, thus the biology on biomembrane be it is abundant, except the original of bacterium and a variety of kinds
Outside lively object and metazoa, additionally it is possible to the der Pilz of the stronger Sphaerotilus of oxidability is grown, and without sludge bulking phenomenon
Occur.The stable ecosystem and food chain are capable of forming on biomembrane.
(2) all biomembranes of filler surface gather, and form the main structure of biomembrane, a large amount of due to der Pilz
It breeds, it is possible to form the intensive biological net of a spatially structure, waste water passes through wherein can effectively improve purification
Effect.
(3) due to being aerated, biofilm surface constantly receives aeration stripping, is conducive to the work for keeping biomembrane in this way
Property, the proliferation of anaerobic membrane, is also suitable for the utilization rate for improving oxygen always, therefore is able to maintain the active biomass of higher concentration.Just
Because of that A/O can receive higher organic loading, treatment effeciency is higher, is conducive to reduce reaction pool volume and land occupation face
Product.
2, the feature of operation aspect: impact load has stronger adaptability, under the conditions of intermittent duty, still is able to protect
Good treatment effect is held, to non-uniform enterprise is drained, is more of practical significance；Easy to operate, operation is convenient, easy to maintain
Management, does not need sludge reflux, does not generate sludge bulking phenomenon；Sludge creation amount is few, and mud granule is larger, is easy to precipitate.
3, the feature in terms of function: there are a variety of purification functions such as to run proper except organic contamination beyond the region of objective existence is effectively removed
Can also be to denitrogenation and dephosphorization, therefore can be used as tertiary treatment technology.
A/O saves occupied area, and operation is convenient, and process flow is simpler；Easy to operate, easy to maintain and management passes through
Biofilm content of microorganisms is high, and the adaptable, high treating effect to difficult waste water.
Step 7: precipitating and flocculation sedimentation
Treated that composite waste is introduced into secondary settling tank is precipitated for catalytic oxidation, then sequentially enters level-one flocculation sedimentation tank
Two-stage flocculation sedimentation is carried out with second level flocculation sedimentation tank, removes wherein insoluble substance, the sludge and two generated in secondary settling tank
The sludge generated in grade flocculation sedimentation tank enters sludge concentration tank.
Step 8: the composite waste after flocculation sedimentation, which enters ozone oxidation pond, carries out oxidation processes；It is mixed after ozone oxidation
Conjunction waste water enters biological aerated filter and carries out aeration degrading waste water COD, is tested by biological aerated filter, examines whether COD reaches
Mark, discharge after COD is up to standard.
Step 9: a set of ammonia spirit chemicals dosing plant that disappears is arranged after biological aerated filter, is used for when ammonia nitrogen index needs to adjust
Remove ammonia nitrogen in waste water.
Step 10: Treatment of Sludge
The sludge in the sludge and two-stage flocculation sedimentation tank in sludge, secondary settling tank during oxidation of formaldehyde enters sludge
Concentration basin, the supernatant of sludge concentration tank enter step the balancing reservoir in (3), and the sludge in sludge concentration tank is through plate and frame filter press
The sludge outward transport generated after compression, outer processing of entrusting
The sludge generated in sewage treatment is concentrated through sludge concentration tank and collects, and transports outward after being dehydrated by plate and frame filter press.
Operating cost estimation
One, benzyl dichloride oxidation of formaldehyde
1, waste water 35m after neutralizing3/ day, medicament expense: hydrogen peroxide 2%, 2000 yuan/ton of unit price；Conversion medicament expense: 1400 yuan/
It.
Two, sulfonic acid aldehyde (mother liquor) waste water: 12m3
Three, it forces to follow bad
1, high-salt wastewater: waste water 35m after benzyl dichloride neutralizes3；Waste water 12m after the concentration of sulfonic acid aldehyde3, add up to 47m3.Feed (MVR
Force) 3.6m per hour3, conversion elapsed time: 13 hours.
2, steam needs 0.2 ton of steam by 198 yuan/ton of calculating per hour, daily operation 13 hours, and conversion consumption steam takes:
515 yuan/day.
3, electric installed capacity is 235kw, and operation is calculated according to 180kw, and the electricity charge are according to 0.8 yuan/Kw, and operation 13 is small daily
When, conversion consumption energy charge: 1872 yuan/day.
Four, flocculation reaction, biochemical treatment, advanced treating operation
1, according to daily 260m3Waste water, consumption PAC is 78kg, pAM 0.26kg, converted expenses are as follows: 135 yuan/day.
2, electricity, ozone generator installed capacity 75kw, other 120kw, run power 150kw, and electricity presses 0.8 yuan/kw, conversion
Electricity cost: 1020 yuan/day.
3, sludge, the ammonia spirit that disappears are by 500 yuan/day.
Five, labour cost
10 people of sewage plant (including MVR is forced and MVR falling liquid film) staffing, personnel's wage, 180 yuan for each person every day.Conversion
Daily labour cost: 1800 yuan.
Add up to daily sewage treatment expense: 7242 yuan, handling sewage 110m according to daily3It calculates, converts ton wastewater treatment
Expense are as follows: 65.84 yuan, cost for wastewater treatment is very low.
Embodiment 3
In fluorescent whitening agent AMS production process, the waste water that filters pressing workshop section generates is stored through workshop collecting pit, passes through elevator pump
Squeeze into sewage plant collecting-tank through " neutralization+centrifugation+oxidation of formaldehyde device+MVR+ balancing reservoir+UASB+ hydrolysis acidification+catalytic oxidation+
Secondary settling tank+second level flocculation reaction+ozone oxidation+disappears ammonia spirit device+discharge pond ", handle it is up to standard after discharge garden sewage treatment plant.
The filter residue that project filters pressing generates, as dangerous waste, outer processing of entrusting.
Embodiment 4
In fluorescent whitening agent APC production process, the waste water that nanofiltration workshop section generates is stored through workshop collecting pit, passes through elevator pump
Squeeze into sewage plant collecting-tank through " neutralization+centrifugation+oxidation of formaldehyde device+MVR+ balancing reservoir+UASB+ hydrolysis acidification+catalytic oxidation+
Secondary settling tank+second level flocculation reaction+ozone oxidation+disappears ammonia spirit device+discharge pond ", handle it is up to standard after discharge garden sewage treatment plant.
The filter residue that project filters pressing generates, nanofiltration membrane of giving up is as dangerous waste, outer processing of entrusting.
Embodiment 5
In 357 production process of fluorescent whitening agent, the waste water that nanofiltration workshop section generates is stored through workshop collecting pit, passes through elevator pump
Squeeze into sewage plant collecting-tank through " neutralization+centrifugation+oxidation of formaldehyde device+MVR+ balancing reservoir+UASB+ hydrolysis acidification+catalytic oxidation+
Secondary settling tank+second level flocculation reaction+ozone oxidation+disappears ammonia spirit device+discharge pond ", handle it is up to standard after discharge garden sewage treatment plant.
The filter residue that project filters pressing generates, nanofiltration membrane of giving up is as dangerous waste, outer processing of entrusting.
Taking the above-mentioned ideal embodiment according to the present invention as inspiration, through the above description, relevant staff is complete
Various changes and amendments can be carried out without departing from the scope of the technological thought of the present invention' entirely.The technology of this invention
Property range is not limited to the contents of the specification, it is necessary to which the technical scope thereof is determined according to the scope of the claim.
Claims (7)
1. producing the processing method of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde, it is characterised in that: including following step
It is rapid:
(1) the fluorescer waste water that the benzyl dichloride waste water and production fluorescer generated first to production biphenyl-benzyl dichloride generates carries out
Neutralization reaction makes ph=7, and the benzyl dichloride waste water after neutralization is centrifuged using centrifuge, removes zinc-containing sludge therein；
(2) benzyl dichloride waste water and fluorescer waste water after removing zinc mud enter oxidation of formaldehyde device and are aoxidized, in oxidation process
Middle addition concentration is 1%-3% hydrogen peroxide, removes formaldehyde and salts substances in waste water, benzyl dichloride waste water and glimmering after being pre-processed
Photo etching waste water, the sludge that oxidation of formaldehyde process generates enter sludge concentration tank；
(3) waste water of benzyl dichloride waste water and fluorescer waste water after the evaporation of MVR falling film evaporator enters balancing reservoir after pre-processing, raw
Produce ortho-sulfonic acid sodium benzaldehyde and waste water after the evaporation of MVR forcing vaporiser of the sulfonic acid aldehyde waste water that generates, workshop appliance flushing water,
Waste water, which enters in balancing reservoir, after sanitary sewage and flocculation sedimentation is mixed, and composite waste is obtained；
(4) composite waste enters upflow anaerobic sludge blanket reactor UASB progress anaerobic reaction, removes having in composite waste
Machine object；
(5) composite waste after UASB Anaerobic Treatment sequentially enters hydrolysis acidification pool and contact-oxidation pool, be hydrolyzed acidification and
Catalytic oxidation processing further removes the organic matter in composite waste；
(6) treated that composite waste is introduced into secondary settling tank is precipitated for catalytic oxidation, then sequentially enters level-one flocculation sedimentation tank
Two-stage flocculation sedimentation is carried out with second level flocculation sedimentation tank, removes wherein insoluble substance, the sludge and two generated in secondary settling tank
The sludge generated in grade flocculation sedimentation tank enters sludge concentration tank；
(7) composite waste after flocculation sedimentation enters ozone oxidation pond progress oxidation processes；
(8) composite waste after ozone oxidation enters biological aerated filter and carries out aeration degrading waste water COD, is filtered by aeration and biological
Whether pond experiment, examine COD up to standard, discharge after COD is up to standard；
(9) supernatant of sludge concentration tank enters step the balancing reservoir in (3), and the sludge in sludge concentration tank is through plate and frame filter press
The sludge outward transport generated after compression, outer processing of entrusting.
2. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
Be characterized in that: benzyl dichloride waste water is transferred to PH to 3 by the liquid alkaline for being first 30-40% with concentration in step (1), then is adjusted and given up with soda ash
Water pH to 7.
3. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
It is characterized in that: in step (3), waste water, workshop appliance flushing water, life of the p-sulfonic acid aldehyde waste water after the evaporation of MVR forcing vaporiser
Waste water carries out homogenization after sewage living and flocculation sedimentation.
4. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
Be characterized in that: in step (7), the gas production of the ozone generator in ozone oxidation pond is 3kg/h.
5. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
It is characterized in that: a set of ammonia spirit chemicals dosing plant that disappears is set after the biological aerated filter in step (8), remove the ammonia nitrogen in waste water.
6. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
Be characterized in that: the evaporation rate of MVR falling film evaporator is 6.8t/h, and the evaporation rate of MVR forcing vaporiser is 3.0t/h.
7. the processing method of production biphenyl-benzyl dichloride according to claim 1 and the produced sewage of ortho-sulfonic acid sodium benzaldehyde,
Be characterized in that: in step (3), the evaporating temperature of MVR forcing vaporiser is set as 85 DEG C, after secondary steam is compressed, and temperature can rise
Height arrives 90-95 DEG C.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111908740A (en) * | 2020-09-06 | 2020-11-10 | 山东蓝城分析测试有限公司 | Method for treating wall imitation stone coating wastewater |
| CN112174422A (en) * | 2019-07-02 | 2021-01-05 | 南京绿岛环境工程有限公司 | Physicochemical and biochemical treatment process for high-salt high-COD cellulose ether production wastewater |
| CN116239264A (en) * | 2023-03-24 | 2023-06-09 | 吴桥县六合德利化工有限责任公司 | Waste water recovery process for preparing sodium o-sulfonate benzaldehyde |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1792894A (en) * | 2005-11-17 | 2006-06-28 | 中国地质大学（武汉） | Process for treating yellow ginger saponin waste water by hydrochloric acid method |
| CN101423313A (en) * | 2008-11-14 | 2009-05-06 | 山西大学 | Fluorescent whitening agent production waste water treatment process |
| CN102115291A (en) * | 2009-12-31 | 2011-07-06 | 凯特琳·陈晓英 | Process for treating high-concentration organic wastewater difficult to degrade |
| CN102515437A (en) * | 2011-12-21 | 2012-06-27 | 江苏省环境科学研究院 | Chemical industry park's wastewater bio-treatment apparatus and method thereof |
| CN103755103A (en) * | 2014-01-24 | 2014-04-30 | 广州市市政工程设计研究院 | LCD (liquid crystal display) industrial wastewater advanced treatment technology |
-
2019
- 2019-01-17 CN CN201910044366.1A patent/CN109851161B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1792894A (en) * | 2005-11-17 | 2006-06-28 | 中国地质大学（武汉） | Process for treating yellow ginger saponin waste water by hydrochloric acid method |
| CN101423313A (en) * | 2008-11-14 | 2009-05-06 | 山西大学 | Fluorescent whitening agent production waste water treatment process |
| CN102115291A (en) * | 2009-12-31 | 2011-07-06 | 凯特琳·陈晓英 | Process for treating high-concentration organic wastewater difficult to degrade |
| CN102515437A (en) * | 2011-12-21 | 2012-06-27 | 江苏省环境科学研究院 | Chemical industry park's wastewater bio-treatment apparatus and method thereof |
| CN103755103A (en) * | 2014-01-24 | 2014-04-30 | 广州市市政工程设计研究院 | LCD (liquid crystal display) industrial wastewater advanced treatment technology |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112174422A (en) * | 2019-07-02 | 2021-01-05 | 南京绿岛环境工程有限公司 | Physicochemical and biochemical treatment process for high-salt high-COD cellulose ether production wastewater |
| CN111908740A (en) * | 2020-09-06 | 2020-11-10 | 山东蓝城分析测试有限公司 | Method for treating wall imitation stone coating wastewater |
| CN116239264A (en) * | 2023-03-24 | 2023-06-09 | 吴桥县六合德利化工有限责任公司 | Waste water recovery process for preparing sodium o-sulfonate benzaldehyde |
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