CN109607979A - Treatment method for high-salinity wastewater - Google Patents
Treatment method for high-salinity wastewater Download PDFInfo
- Publication number
- CN109607979A CN109607979A CN201910067299.5A CN201910067299A CN109607979A CN 109607979 A CN109607979 A CN 109607979A CN 201910067299 A CN201910067299 A CN 201910067299A CN 109607979 A CN109607979 A CN 109607979A
- Authority
- CN
- China
- Prior art keywords
- salt
- mother liquor
- evaporator
- wastewater
- mvr evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/03—Pressure
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/282—Anaerobic digestion processes using anaerobic sequencing batch reactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention discloses a kind for the treatment of method for high-salinity wastewater, belong to technical field of sewage, including high-salt wastewater preheating-evaporation separation-saliferous mother liquid disposal, the secondary steam of MVR evaporator is connected through vapour compression machine with heat exchanger, saturated salt mother liquor enters cyclone separator, and the centrifugate of cyclone separator is recycled to MVR evaporator, thickening salting liquid sequentially enters magma tank and centrifuge；The part saliferous mother liquor reflux of centrifuge is recycled to outside MVR evaporator, part saliferous mother liquor through heat pump and heat exchanger to be drained into scrapper thin film evaporator and is evaporated, and scrapper thin film evaporator steam, which carries organic matter and enters sewage plant after waste heat recycling condensation, to be handled.The present invention utilizes the combination of MVR evaporator and scrapper thin film evaporator, solve the problems, such as that high boiling point organic compound enrichment leads to the reduction of solid salt quality, entire evaporative desalination process is operated continuously, solid salt quality is improved, the desalting processing of every profession and trade high-salt wastewater can be widely applied to.
Description
Technical field
The invention belongs to technical field of sewage more particularly to a kind for the treatment of method for high-salinity wastewater.
Background technique
Currently, numerous chemical companies can generate a large amount of wastewater from chemical industry in process of production, a portion saliferous is higher
Wastewater treatment difficulty is larger, such as since saliferous is higher in dyestuff, pesticide, medicine intermediate waste water, seriously polluted, it is necessary to desalination
Processing could discharge.Moreover such waste component is complicated, does not have recovery value, using either physically or chemically higher cost,
Therefore biological treatment is still preferred method.
It is that 0.8% or so and less salt waste water below, part are micro- that conventional biological treatment process waste water, which is generally salinity,
Biology after taming can tolerate salinity be 1%-2% waste water, but be not amenable to variation water quality impact, and run it is bad when need to throw
Facultative Halophiles are added to increase ton cost of water treatment, stable water outlet is difficult to ensure, and chemical production wastewater salinity is generally 5% or more
To between 20%.Therefore, the biological treatment needs of high slat-containing wastewater are diluted, and usually (salinity is less than under low salt concn
1%) it runs, causes the waste of water resource, treatment facility is huge, investment increases, and operating cost improves.It needs to carry out waste water thus
Desalting processing derives various ways for waste water desalination: steamer, multiple-effect evaporation, single effect evaporation and MVR mechanical steam are pressed again
The technologies such as contracting are to carry out physics desalination, area in such a way that heating evaporation water carries out the final abjection inorganic salts of material concentration
It is not that its energy consumption, efficiency, equipment investment are different.
Enrichment high boiling point organic compound saliferous mother liquor is generated during evaporative desalination, due to the high evaporation capacity of partial organic substances boiling point
It is small and be enriched in mother liquor, and it is final be enriched with to a certain degree after due to commonly evaporate high boiling point organic compound cannot be steamed be mixed into it is solid
In body salt, to influence the quality, color and purity that finally evaporate salt, it is mixed into the solid salt of high boiling point organic compound or even becomes
Dangerous waste need to entrust dangerous waste relevant unit to be disposed, and increase dangerous waste related management, storage, transport, labour, account etc. at
This consumption greatly increases entreprise cost.
Summary of the invention
The object of the present invention is to provide a kind for the treatment of method for high-salinity wastewater, it is intended to solve above-mentioned high-salt wastewater in the prior art
Enrichment high boiling point organic compound saliferous mother liquor is generated during evaporative desalination, influence finally to evaporate the quality of solid salt, color and
Purity, the solid salt for being mixed into high boiling point organic compound can become the technical issues of dangerous waste increases cost of disposal.
In order to solve the above technical problems, the technical solution used in the present invention is:
A kind for the treatment of method for high-salinity wastewater, comprising the following steps:
A, high-salt wastewater preheats: the high-salt wastewater that salinity is 5%-20% being intake and is preheating to 50-80 DEG C by room temperature；
B, evaporation separation: the high-salt wastewater after pre-heating temperature elevation enters MVR evaporator and is evaporated concentration, and MVR evaporator initial stage opens
Steam pressure needed for dynamic is 0.2-0.3MPa, and temperature is 110-130 DEG C, and the evaporating temperature that high-salt wastewater is arranged in operational process is
60-98℃；
In evaporating concentration process, moisture and low-boiling-point organic compound are steamed with steam, are formed secondary steam and are entered vapour compression machine
Compression heating, it is in heat pump cycle liquid heating supplement MVR evaporator that the secondary steam institute band heat after heating exchanges heat through heat exchanger
Institute, separation chamber calorific requirement is evaporated, solution evaporating temperature in evaporation separation chamber is maintained；
Material salt concentration after the concentration of MVR evaporator is thickened after reaching saturation state into cyclone separator, is centrifuged
Liquid is back to MVR evaporator, the high level salt solution after thickening enter magma tank crystallization after, recycle centrifuge isolate moisture content≤
4% solid salt and saliferous mother liquor；
C, saliferous mother liquid disposal: centrifuge is centrifuged the solution after desalination and forms saliferous mother liquor, and saliferous mother liquor outlet a part is remaining
Saliferous mother liquor reflux to MVR evaporator continues to apply；Outlet mother liquor amount accounts for saliferous mother liquor 3%-8%, and outlet mother liquor is thin using scraper plate
Film evaporator continues to evaporate, and is concentrated to get solid salt；Enter sewage after the condensate liquid UTILIZATION OF VESIDUAL HEAT IN of scrapper thin film evaporator
Station is handled；
Preferably, the saliferous concentrate of the MVR evaporator distributes a part after heat pump and heat exchanger heating through branch pipe
It is recycled to MVR evaporator, secondary steam enters condensate liquid after entering heat exchanger heat exchange condensation after vapour compression machine compression heating
Tank.
Preferably, the water inlet of the condensate liquid of the condensate drum and high-salt wastewater carries out heat exchange, the condensation after heat exchange
Water reuse enters sewage plant processing.
Preferably, the not condensing of the condensate drum carries out heat exchange, heat through the water inlet of vacuum pump extraction and high-salt wastewater
Recycling condensing water or entrance sewage plant after exchange are handled, and the fixed gas after heat exchange enters exhaust treatment system.
Preferably, the vapour compression machine is Roots Compressor or centrifugal compressor.
Preferably, blender is equipped in the magma tank.
Preferably, the sewage plant include the conditioning tank being sequentially communicated, Anaerobic Sequencing Bath Reactor, anaerobic pond, anoxic pond,
Aerobic tank, secondary settling tank are connected to UASB reactor, and the mixed liquor of the anoxic pond is back to anaerobic pond, the mixing of the aerobic tank
Liquid is back to anoxic pond, the activity sludge reflux of the secondary settling tank to anoxic pond.
Preferably, the boosted pond of the supernatant of the secondary settling tank and delivery pump are delivered to UASB reactor.
The beneficial effects of adopting the technical scheme are that compared with prior art, the present invention is evaporated by MVR
Device saves a large amount of steam sources using secondary steam recompression, saves operating cost, the saturated salt mother liquor after being centrifuged desalination
Into MVR evaporator circulating and evaporating, fractional saturation salt mother liquor outlet is carried out being evaporated processing into scrapper thin film evaporator, be avoided
Organic matter is enriched with bring negative effect (evaporation capacity reduces, energy consumption increases, goes out salt quality), and scrapper thin film evaporator steam carries
Organic matter enters plant area's sewage plant after waste heat recycling condensation and carries out sewage treatment.The present invention is thin using MVR evaporator and scraper plate
The combination of film evaporator solves the problems, such as that high boiling point organic compound enrichment causes the reduction of solid salt quality, makes entirely to evaporate de-
The continuous operation of salt process, improves solid salt quality, can be widely applied to the desalting processing of every profession and trade high-salt wastewater.
Detailed description of the invention
The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.
Fig. 1 is a kind of process flow chart for the treatment of method for high-salinity wastewater provided in an embodiment of the present invention；
Fig. 2 is the waste water processes figure of sewage plant in Fig. 1.
Specific embodiment
With reference to the attached drawing in the embodiment of the present invention, technical solution in the embodiment of the present invention carries out clear, complete
Ground description, it is clear that described embodiment is only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
Currently, high-salt wastewater processing mostly uses MVR evaporator, generally applied 20-40 times by Recycling Mother Solution, due to high boiling
Point organic matter evaporation capacity is less and is enriched with, and the enrichment of high boiling point organic compound causes solution elevation of boiling point evaporation capacity to decline, high boiling
Select organic matter enrichment evaporate afterwards to a certain extent the salt of abjection due to impurity high boiling point organic compound is excessive and it is faint yellow to show or
Yellow influences the quality, appearance and purity of salt, and the standard for no longer meeting Nacl cannot be sold outside, or even need to entrust as dangerous waste
Dangerous waste qualification unit is disposed, and greatly increases business processes cost.
It is able to solve the above problem using the present invention, the process flow for the treatment of method for high-salinity wastewater provided by the invention is as schemed
Shown in 1, the treatment method for high-salinity wastewater, comprising the following steps:
A, high-salt wastewater preheats: the high-salt wastewater that salinity is 5%-20% being intake and is preheating to 50-80 DEG C by room temperature；High-salt wastewater
It is preferred that mono-salt waste water (containing only a kind of inorganic salts ingredients), if containing plurality of inorganic salt salty separation and essence should be carried out by increasing equipment
System, otherwise needs to be disposed by dangerous waste.
B, evaporation separation: the high-salt wastewater after pre-heating temperature elevation enters MVR evaporator and is evaporated concentration, at the beginning of MVR evaporator
Steam pressure needed for phase starts is 0.2-0.3MPa, and temperature is 110-130 DEG C, and the evaporation temperature of high-salt wastewater is arranged in operational process
Degree is 60-98 DEG C；
In evaporating concentration process, moisture and low-boiling-point organic compound are steamed with steam, are formed secondary steam and are entered vapour compression machine
Compression heating, it is in heat pump cycle liquid heating supplement MVR evaporator that the secondary steam institute band heat after heating exchanges heat through heat exchanger
Institute, separation chamber calorific requirement is evaporated, solution evaporating temperature in evaporation separation chamber is maintained；The saliferous concentrate of MVR evaporator is through branch pipe point
Outflow a part is recycled to MVR evaporator by heat pump and heat exchanger.Wherein, MVR evaporator is by falling film evaporator and/or pressure
Circulating evaporator is composed, according to material characteristic select evaporator type, material characteristic include fouling wall built-up, evaporating temperature and
Material concentration etc..
High-salt wastewater material is concentrated in MVR evaporator, and concentration increases, and moisture and low-boiling-point organic compound are with steamed
Out, cyclone separator being entered after material salt concentration reaches saturation state to be thickened, centrifugate is back to vapor seperator,
High level salt solution after thickening enters magma tank, and being stirred continuously in magma tank equipped with blender prevents crystallization wall built-up, recycles centrifugation
The solid salt that machine isolates moisture content≤4% is packed and stored；The saliferous mother liquor isolated enters step C and is further processed.
High-salt wastewater preferred concentration is the brine waste of 10%-20%, and the brine waste that salinity is 5%-10% is increase
Desalination operation continuity and reduction energy consumption, can increase enriched chamber before the evaporation separation chamber of MVR evaporator, can be falling film evaporation
Room, climbing-film evaporation room, circulating and evaporating room etc. are concentrated, and determine type with specific reference to the type and experiment lab scale of waste water and salt.
Condensate liquid into condensate drum is pumped into heat exchange equipment one by delivery pump, in heat exchange equipment one and high-salt wastewater
Water inlet carry out heat exchange, play the role of preheating high-salt wastewater, recycling condensing water after heat exchange or enter sewage plant and handle.
Secondary steam enters heat exchanger heat exchange condensation after vapour compression machine compression heating, forms condensate liquid and enters condensate drum, is formed
Condensed water salt content≤1000ppm, waste heat as high-salt wastewater water inlet preheating be discharged at sewage plant after again
Reason.
The not condensing of the condensate drum is carried out using the water inlet that vacuum pump is drawn through heat exchange equipment two and high-salt wastewater
Heat exchange is played the role of preheating high-salt wastewater, and the recycling condensing water or entrance sewage plant after heat exchange are handled, after heat exchange
Remaining fixed gas enters exhaust treatment system.
Wherein, heat exchange equipment one and heat exchange equipment two select plate heat exchanger；Heat exchanger selects pipe heat exchanger.
C, saliferous mother liquid disposal: centrifuge is centrifuged the solution after desalination and forms saliferous mother liquor, and saliferous mother liquor outlet is a part of,
Remaining saliferous mother liquor reflux to MVR evaporator continues to apply；Outlet mother liquor amount accounts for saliferous mother liquor 3%-8%, and outlet mother liquor is utilized and scraped
Plate thin film evaporator continues to evaporate, and is concentrated to get solid salt；Enter after the condensate liquid UTILIZATION OF VESIDUAL HEAT IN of scrapper thin film evaporator
Sewage plant is handled；
The condensation fluid residual heat recycling pair of the waste heat, scrapper thin film evaporator of the condensate liquid and fixed gas of MVR evaporator secondary steam
The water inlet of high-salt wastewater is preheated, since secondary steam condensate liquid accounting is larger and 85-95 DEG C of secondary steam condensate temperature,
So secondary steam condensate liquid plays main heat exchange thermogenic action, high-salt wastewater water inlet is preheating to 50-80 DEG C by room temperature, is used
Plate heat exchanger is all made of in the heat exchange equipment two of fixed gas preheating and the heat exchange equipment one for condensed water preheating；Secondary steam
It is carried out after compression heating by the saliferous concentrate that the saliferous mother liquor and MVR evaporator of pipe heat exchanger and reflux are diverted
Heat exchange heating.
The vapour compression machine is preferably Roots Compressor or centrifugal compressor, when treating capacity less than 5 tons/constantly adopt
With Roots Compressor, centrifugal compressor is otherwise selected.
Scrapper thin film evaporator hull outside is internal that rotatable scraper plate is housed equipped with heating steam jacket, scraper plate by
The rotary shaft of cylinder center drives.After outlet mother liquor is tangentially added by evaporator top, in the drive of gravity and rotor segment
Under, the film of backspin is formed along the inner wall of shell, by control inlet amount and live steam additional amount, outlet mother liquor can be steamed
It is dry, solid product salt is directly obtained in bottom, secondary steam is then discharged after demister by top.Scrapper thin film evaporator is dashed forward
Advantage is very strong to the adaptability of material out, and thermal resistance influences small, and heat transfer coefficient is big, to high viscosity, easily crystallization, easy fouling, high boiling
Point, high viscosity or the product easily crystallized (loose state particle) containing suspended matter or have the evaporation of thermal sensitivity feed liquid concurrently and are applicable in.Due to
Material is constantly spread to film by the movement of scraper plate on evaporating surface, to achieve the effect that thin film evaporation；Steam is common heat
Medium can reduce the boiling point of material, enhance the effect of evaporation, can directly obtain solid product.Utilize scraper plate film
High boiling point organic compound in outlet mother liquor can further be evaporated by evaporator, grasp entire evaporative desalination process continuously
Make, improve out the quality of solid salt, solves the problems, such as that high boiling point organic compound enrichment quality reduces, can be widely applied to each
Enter sewage plant treatment facility after the desalting processing of industry high-salt wastewater, evaporation condensate and fixed gas UTILIZATION OF VESIDUAL HEAT IN, avoids dirt
Contaminate environment.
It is preferably exactly scheme as shown in Fig. 2, the sewage plant includes the conditioning tank being sequentially communicated, anaerobic as one kind
Formula reactor, anaerobic pond, anoxic pond, aerobic tank, secondary settling tank are connected to UASB reactor, and the mixed liquor of the anoxic pond is back to
Anaerobic pond, the mixed liquor of the aerobic tank are back to anoxic pond, the activity sludge reflux of the secondary settling tank to anoxic pond.Wherein,
The boosted pond of the supernatant of the secondary settling tank and delivery pump are delivered to UASB reactor, the row up to standard after UASB reactor for treatment
It puts.
Enter sewage plant using the condensate wastewater after above-mentioned treatment method for high-salinity wastewater evaporative desalination to handle.The master of waste water
Wanting source is MVR evaporator evaporation condensate waste water and scrapper thin film evaporator evaporative condenser waste water and sanitary sewage and vehicle
Between alkalinity after nitrogen oxides tail gas absorption containing nitrate absorb waste water, since condensate temperature is at 70 ~ 80 DEG C, mix other useless
Water natural cooling enters biochemical treatment system after being cooled to 30 DEG C ~ 35 DEG C, and temperature fall time just combines anaerobic sequencing batch to react
The not flooding time of device, sewage quality after whole mixing are as follows: CODcr value 10000mg/L or so, 200 ~ 300mg/L of ammonia nitrogen and
Part organic nitrogen, 6000 ~ 8000mg/L of nitrate, through system shown in Fig. 2 processing after UCT Process for Effluent CODcr300 ~
500mg/L, 30 ~ 60mg/L of ammonia nitrogen are lifted into UASB reactor and carry out biodegrade and denitrogenation, and UASB is anti-under normal temperature state
It answers device to be discharged CODcr < 150mg/L 10 ~ 20mg/L of ammonia nitrogen, meets integrated wastewater discharge standard stabilization and meet comprehensive row's secondary standard,
Dissolved oxygen gradient is successively decreased between aerobic tank control 0.7 ~ 1.8mg/L of dissolved oxygen, and end dissolved oxygen is minimum, and return sludge ratio 50% ~ 100% is good
Oxygen return current ratio of the mixed liquid 150% ~ 250%, anoxic return current ratio of the mixed liquid 50% ~ 100%.
Anaerobic Sequencing Bath Reactor (Anaerobic Sequencing BatchReactor abbreviation ASBR) is the U.S.
Dague teaches a kind of high-rate anaerobic reactor developed in early 1990s.ASBR is the unstable state anaerobism of intermittent duty
Bioreactor, each cycle of operation were divided into water, reaction, precipitating, draining, standby 5 stages.ASBR anaerobism is compared to other
Anaerobic technique has the advantage that
A. simple process integrates water inlet reaction sedimentation and drawing, and three phase separator is no longer the core of this technique, is not required to additional
Clarifying basin and sedimentation basin, no sludge reflux.
B. the stage of reaction can keep higher upflow velocity 1-5m/h without considering that flow velocity crosses mud of hurrying up due to not being discharged
The generation of phenomenon, contributes to form granule sludge.
C. batch mode of operation, strong shock resistance, other anaerobic techniques are since continuum micromeehanics are discharged while must be equipped with
Otherwise water outlet band mud is caused sludge concentration to reduce by optimal three phase separator, and water quality and quantity changes three-phase separate when fluctuating huge
Will deviate from former design size from the Angular Dimension of device, be likely to result in collecting methane be not thorough, sludge retention it is ineffective.
D. adaptable, it is thoroughly mixed mode, sludge concentration is high, adapts to impact load and high concentrated organic wastewater.
E. flexible operation is run, it can be according to the variation of waste water water, water quality, by adjusting each work in a cycle of operation
Runing time and HRT, SRT of sequence and the requirement for meeting effluent quality have very strong operating flexibility.
F. good effect of separating solid from liquid, out clarification of water.It is separated by solid-liquid separation and is carried out in inside reactor, be that ASBR technique is different from it
One notable feature of his anaerobic technique.Firstly, the flocculation of anaerobic organism group is similar with the mode of aerobic activated sludge process, it is by thin
Bacterium causes the Finite Concentration of matrix, and F/M value has a major impact it.Low F/M value is conducive to bioflocculation, and sedimentation is fast, water outlet
Suspended solid is low.When the anaerobic reactor steady state operation that one continuous feed is thoroughly mixed, F/M is certain value, and intermittently operated
ASBR reactor water inlet after be high F/M, with the progress of reaction, F/M is gradually decreased, reaction terminate draining when, F/M is minimum,
And gas production is minimum, the interference for the upflow velocity for being easy to be separated by solid-liquid separation, and not intaking, pure gravitational settling.Therefore, from solid-liquid point
Say that the batch mode of operation of ASBR method is better than the continuous operation mode of other anaerobic process from maintenance high concentration sludge effect.
Anaerobic pond, anoxic pond, aerobic tank and the UCT technique for promoting pond composition, UCT technique (University of in Fig. 2
It Capetown) is a kind of denitrification dephosphorization technique of the Cape Town, RSA university exploitation similar to A2/O technique.UCT technique and A2/O work
Skill can be prevented due to nitrate in this way the difference is that clarifier sludge flows back into anoxic pond rather than flows back into anaerobic pond
Nitrogen enters anaerobic pond, destroys the anaerobic state of anaerobic pond and influences the dephosphorizing rate of system, increases from anoxic pond to anaerobic pond
Mixed liquor flows back, and more dissolubility BOD is contained in the mixed liquor to flow back from anoxic pond to anaerobic pond, and nitrate is seldom, subtracts
Few dissolved oxygen and entering for nitrate build good anaerobic environment, are provided by the hydrolysis of organic matter reaction carried out in anaerobism section
Optimal condition, gives full play to hydrolysis, the acidification of anaerobic technique, organic matter is decomposed into small point of easy biochemical degradation
Son, anoxic pond carry out nitrification liquid reflux and carry out biological denitrificaion reaction, and the nitrate nitrogen of aerobic tank, nitrite nitrogen are carried out denitrification and taken off
Nitrogen out, aerobic tank carry out the degradation of organic matter and the nitration reaction of ammonia nitrogen by control dissolved oxygen, residence time, reflux ratio.
UASB reactor is de- using the degradation of the reactor of anaerobic UASB and facultative anaerobic bacteria progress organic matter and biology
Nitrogen, in the lower nitrate containing ammonia nitrogen of organic concentration, UASB reactor can carry out denitrification denitrogenation using facultative anaerobic bacteria,
Anti-nitration reaction is carried out in a manner of UASB continuum micromeehanics, denitrification process is NO3- → NO2- → N2, micro- life in anti-digestion process
C, N element needed for object obtains energy and cell synthesis by the degradation of organic matter and ammonia nitrogen, reach discharge standard.
In conclusion the present invention is particularly suitable for mono-salt for processing high-salt wastewater containing organic matter (salt content 5%-20%)
Waste water (a kind of only inorganic salts ingredients), low-boiling-point organic compound is successively cold through heat exchanger with steam in evaporation process in high-salt wastewater
Subsequent sewage plant is discharged into after solidifying, preheating high-salt wastewater water inlet to be handled；MVR evaporator utilizes secondary steam recompression
Save a large amount of steam sources, save operating cost, high-salt wastewater after MVR evaporator evaporation and concentration, into cyclone separator from
Saturated salt mother liquor after heart desalination enters back into vapor seperator circulating and evaporating, fractional saturation salt mother liquor outlet, into scraper plate film
Evaporator carries out being evaporated processing, and the control of outlet mother liquid disposal amount is 5% or so, to avoid organic matter enrichment bring negative effect
(evaporation capacity reduces, energy consumption increases, goes out salt quality), scrapper thin film evaporator steam enters plant area's sewage after waste heat recycling condensation
It stands and carries out sewage treatment, last qualified discharge.
Many details are elaborated in the above description to facilitate a thorough understanding of the present invention, still the present invention can be with
Implemented using other than the one described here other way, those skilled in the art can be without prejudice to intension of the present invention
In the case of do similar popularization, therefore the present invention is not limited by particular embodiments disclosed above.
Claims (8)
1. a kind for the treatment of method for high-salinity wastewater, which comprises the following steps:
A, high-salt wastewater preheats: the high-salt wastewater that salinity is 5%-20% being intake and is preheating to 50-80 DEG C by room temperature；
B, evaporation separation: the high-salt wastewater after pre-heating temperature elevation enters MVR evaporator and is evaporated concentration, and MVR evaporator initial stage opens
Steam pressure needed for dynamic is 0.2-0.3MPa, and temperature is 110-130 DEG C, and the evaporating temperature that high-salt wastewater is arranged in operational process is
60-98℃；
In evaporating concentration process, moisture and low-boiling-point organic compound are steamed with steam, are formed secondary steam and are entered vapour compression machine
Compression heating, it is in heat pump cycle liquid heating supplement MVR evaporator that the secondary steam institute band heat after heating exchanges heat through heat exchanger
Institute, separation chamber calorific requirement is evaporated, solution evaporating temperature in evaporation separation chamber is maintained；
Material salt concentration after the concentration of MVR evaporator is thickened after reaching saturation state into cyclone separator, is centrifuged
Liquid is back to MVR evaporator, the high level salt solution after thickening enter magma tank crystallization after, recycle centrifuge isolate moisture content≤
4% solid salt and saliferous mother liquor；
C, saliferous mother liquid disposal: centrifuge is centrifuged the solution after desalination and forms saliferous mother liquor, and saliferous mother liquor outlet a part is remaining
Saliferous mother liquor reflux to MVR evaporator continues to apply；Outlet mother liquor amount accounts for saliferous mother liquor 3%-8%, and outlet mother liquor is thin using scraper plate
Film evaporator continues to evaporate, and is concentrated to get solid salt；Enter sewage after the condensate liquid UTILIZATION OF VESIDUAL HEAT IN of scrapper thin film evaporator
Station is handled.
2. treatment method for high-salinity wastewater according to claim 1, it is characterised in that: the saliferous of the MVR evaporator is concentrated
Liquid through branch pipe distribute a part by heat pump and heat exchanger heating after be recycled to MVR evaporator, secondary steam is through both vapor compression
Enter condensate drum after entering heat exchanger heat exchange condensation after machine compression heating.
3. treatment method for high-salinity wastewater according to claim 2, it is characterised in that: the condensate liquid and height of the condensate drum
The water inlet of salt waste water carries out heat exchange, and the recycling condensing water or entrance sewage plant after heat exchange are handled.
4. treatment method for high-salinity wastewater according to claim 2, it is characterised in that: the not condensing of the condensate drum is through true
Empty pumping, which goes out, carries out heat exchange with the water inlet of high-salt wastewater, recycling condensing water after heat exchange or enters sewage plant and handles, and heat is handed over
Fixed gas after changing enters exhaust treatment system.
5. treatment method for high-salinity wastewater according to claim 1, it is characterised in that: the vapour compression machine is roots-type pressure
Contracting machine or centrifugal compressor.
6. treatment method for high-salinity wastewater according to claim 1, it is characterised in that: be equipped with blender in the magma tank.
7. treatment method for high-salinity wastewater according to claim 1-6, it is characterised in that: the sewage plant include according to
Conditioning tank, Anaerobic Sequencing Bath Reactor, anaerobic pond, anoxic pond, aerobic tank, the secondary settling tank of secondary connection are connected to UASB reactor,
The mixed liquor of the anoxic pond is back to anaerobic pond, and the mixed liquor of the aerobic tank is back to anoxic pond, the work of the secondary settling tank
Property sludge reflux is to anoxic pond.
8. treatment method for high-salinity wastewater according to claim 7, it is characterised in that: the supernatant of the secondary settling tank is boosted
Pond and delivery pump are delivered to UASB reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910067299.5A CN109607979A (en) | 2019-01-24 | 2019-01-24 | Treatment method for high-salinity wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910067299.5A CN109607979A (en) | 2019-01-24 | 2019-01-24 | Treatment method for high-salinity wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109607979A true CN109607979A (en) | 2019-04-12 |
Family
ID=66017249
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910067299.5A Pending CN109607979A (en) | 2019-01-24 | 2019-01-24 | Treatment method for high-salinity wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109607979A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112028407A (en) * | 2020-09-09 | 2020-12-04 | 姜超 | Method for treating wastewater in production process of hydroxypropyl methyl cellulose |
| CN113024036A (en) * | 2021-03-18 | 2021-06-25 | 河南绿水青山环保科技有限公司 | Wastewater treatment system |
| CN114262111A (en) * | 2021-12-27 | 2022-04-01 | 北京华源泰盟节能设备有限公司 | Softened sewage treatment system of heat exchange station |
| CN114291956A (en) * | 2022-01-21 | 2022-04-08 | 浙江天地环保科技股份有限公司 | Improved MVR device applied to zero discharge of catalyst regeneration wastewater |
| CN114538548A (en) * | 2022-02-25 | 2022-05-27 | 苏州仕净科技股份有限公司 | Low-cost ammonium sulfate waste liquid recycling treatment process |
| CN114684884A (en) * | 2020-12-28 | 2022-07-01 | 江苏嘉泰蒸发设备股份有限公司 | Concentration and decrement process for evaporating and crystallizing high-content organic matters in salt-containing wastewater |
| CN114906895A (en) * | 2022-06-22 | 2022-08-16 | 广东闻扬环境科技有限公司 | Salt-containing wastewater crystallization treatment device and treatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150047965A1 (en) * | 2007-07-24 | 2015-02-19 | Brad M. MALATESTA | Method of cleaning and recycling glycol-tainted water from de-icing operations at airports |
| CN106669207A (en) * | 2017-02-27 | 2017-05-17 | 江苏省环境科学研究院 | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater |
| CN107344785A (en) * | 2017-08-30 | 2017-11-14 | 东华工程科技股份有限公司 | A kind of solventing-out method of embrane method, the hot method group technology processing high strong brine of coal chemical industry |
| CN108358365A (en) * | 2017-11-12 | 2018-08-03 | 吴来贵 | A kind of Waste water concentrating crystallization apparatus |
| CN108689540A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Incineration of refuse flyash wastewater zero discharge and recycling unit and treatment process |
-
2019
- 2019-01-24 CN CN201910067299.5A patent/CN109607979A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150047965A1 (en) * | 2007-07-24 | 2015-02-19 | Brad M. MALATESTA | Method of cleaning and recycling glycol-tainted water from de-icing operations at airports |
| CN106669207A (en) * | 2017-02-27 | 2017-05-17 | 江苏省环境科学研究院 | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater |
| CN108689540A (en) * | 2017-04-12 | 2018-10-23 | 麦王环境技术股份有限公司 | Incineration of refuse flyash wastewater zero discharge and recycling unit and treatment process |
| CN107344785A (en) * | 2017-08-30 | 2017-11-14 | 东华工程科技股份有限公司 | A kind of solventing-out method of embrane method, the hot method group technology processing high strong brine of coal chemical industry |
| CN108358365A (en) * | 2017-11-12 | 2018-08-03 | 吴来贵 | A kind of Waste water concentrating crystallization apparatus |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112028407A (en) * | 2020-09-09 | 2020-12-04 | 姜超 | Method for treating wastewater in production process of hydroxypropyl methyl cellulose |
| CN114684884A (en) * | 2020-12-28 | 2022-07-01 | 江苏嘉泰蒸发设备股份有限公司 | Concentration and decrement process for evaporating and crystallizing high-content organic matters in salt-containing wastewater |
| CN113024036A (en) * | 2021-03-18 | 2021-06-25 | 河南绿水青山环保科技有限公司 | Wastewater treatment system |
| CN114262111A (en) * | 2021-12-27 | 2022-04-01 | 北京华源泰盟节能设备有限公司 | Softened sewage treatment system of heat exchange station |
| CN114291956A (en) * | 2022-01-21 | 2022-04-08 | 浙江天地环保科技股份有限公司 | Improved MVR device applied to zero discharge of catalyst regeneration wastewater |
| CN114538548A (en) * | 2022-02-25 | 2022-05-27 | 苏州仕净科技股份有限公司 | Low-cost ammonium sulfate waste liquid recycling treatment process |
| CN114906895A (en) * | 2022-06-22 | 2022-08-16 | 广东闻扬环境科技有限公司 | Salt-containing wastewater crystallization treatment device and treatment method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109607979A (en) | Treatment method for high-salinity wastewater | |
| CN209555002U (en) | High-salt wastewater processing system | |
| CN102503034B (en) | Treatment method of phenol-containing liquid waste in sebacic acid production | |
| CN101549938B (en) | Method for treating waste water containing high concentration of organosilicon | |
| CN108083552A (en) | A kind of processing method of textile waste | |
| CN102976543A (en) | Garbage leachate disposal method and system | |
| CN111704301A (en) | Landfill leachate treatment process based on PMVR-ZLD | |
| CN112093981B (en) | Sewage treatment device and process for synchronous efficient pollutant removal and comprehensive recycling | |
| Elawwad et al. | Minimization of sludge production in an integrated UASB-continuous flow sequencing batch reactor system | |
| CN112125461A (en) | Comprehensive treatment system and method for high-concentration ammonia nitrogen wastewater | |
| CN109851161B (en) | Treatment method of sewage produced in production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde | |
| CN203173935U (en) | Rubbish leach liquor processing system | |
| CN205347092U (en) | Desulfurization waste water zero release processing system | |
| JP3844347B2 (en) | Method and apparatus for removing and recovering phosphorus from organic wastewater | |
| CN115818880A (en) | Method for treating high-salt high-organic matter high-hardness wastewater | |
| CN110092540A (en) | A kind of water paint waste water treatment system and application method | |
| CN105601031A (en) | Treatment method of waste water produced during production of intermediate compound 4AA | |
| CN112093980B (en) | Efficient nitrogen recovery device and process for sewage | |
| CN115259518A (en) | System and method for treating percolate concentrated solution | |
| CN206033470U (en) | High salt sewage treatment system | |
| CN214360829U (en) | High-efficient nitrogen recovery unit of sewage | |
| CN114835338A (en) | Method for treating percolate concentrated solution of refuse landfill | |
| CN107188378A (en) | Pyrazolone production wastewater treatment device and its handling process | |
| JPH0114836B2 (en) | ||
| CN214829516U (en) | Comprehensive water-saving system for GCL method polycrystalline silicon production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190412 |