CN101224937A - Reuse treating method for chemical industrial plasticizer waste water - Google Patents
Reuse treating method for chemical industrial plasticizer waste water Download PDFInfo
- Publication number
- CN101224937A CN101224937A CNA2008100596476A CN200810059647A CN101224937A CN 101224937 A CN101224937 A CN 101224937A CN A2008100596476 A CNA2008100596476 A CN A2008100596476A CN 200810059647 A CN200810059647 A CN 200810059647A CN 101224937 A CN101224937 A CN 101224937A
- Authority
- CN
- China
- Prior art keywords
- waste water
- water
- enters
- cod
- oil
- 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.)
- Granted
Links
Images
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a recycling and processing method of waste water of a chemical plasticizer, which pertains to the technical field of waste water treatment and resource recycling. The basic proposal is that: the waste water that belongs to high COD (COD is 6000-30000mg/L; BOD is 2000-10000mg/L; pH is 4-12) such as DOG waste water, the caustic washing waster water of epoxy-ester and oil and fats refining waste water, after being respectively pretreated, is mixed with TOTM waste water and enters into a biological and chemical system for processing. The waste water with low COD (COD is 500-2000mg/L; pH is 4-12) is done with aerobic biological treatment after being collected uniformly, then goes through advanced treatment with a membrane method and ozonation catalytic oxidation after coagulation, deposition and filtration and is reused in production. The effluent processed by the invention has stable water quality and can discharge up to standards. The waste water after purification can be reused in production, does not influence the product quality of the plasticizer and has economical and reasonable investment, operation cost and practical and feasible technique.
Description
Technical field
The invention belongs to waste water treatment and resource reusing technical field, relate to the improvement of plasticizer production wastewater and the technological method of recycling, be specially the improvement and the reuse method of DOG waste water, epoxy ester alkali cleaning waste water, oil and fat refining waste water, TOTM waste water and various water coolants.
Background technology
Chemical industry is that China water resources is utilized and one of main industries of consuming, and it needs to use vapo(u)r blasting water, water coolant in process of production and as the production water of all kinds of SOLVENTS etc., is characterized in that water consumption and water displacement are all very big.The various waste water quality water yields of discharging also have very big difference, some water COD concentration is lower, in conjunction with China's water resources recycle of proposition at present and the policy of energy-saving and emission-reduction, the low treated direct discharging of COD waste water of this part is wasted very much, reuse then can produce good economic and social benefit if processing reaches the standard of water of productive use.
Softening agent is a kind of important organic additive in the plastics-production process, and it mainly acts on is to increase plastic plasticity, resin flow when improving forming process, and make product have snappiness.Softening agent is some high boiling points, difficult evaporable thick liquid or low-melting solid normally.According to the difference of chemical structure, softening agent can be divided into phthalic acid ester class, fatty acid ester, phosphoric acid ester, polyester, epoxy ester series and chlorine-containing compound etc.China is the production and consumption big country of softening agent, about 1,000,000 tons of annual throughput.The production process of softening agent can produce the waste water of a large amount of high densitys, contains a large amount of phthalates, polyester and other macromolecule raw material materials in the waste water.This type of waste water has higher toxicity, do not handle direct discharging and will cause environment and have a strong impact on if do not add, simultaneously, because these pollution substance molecular weight are big, complex structure, and contain lopps structures such as benzene more, be difficult to biochemical treatment, so the processing of plasticizer waste water is unusual stubborn problem in the plasticizer production industry development.
At present both at home and abroad to the processing of plasticizer waste water mostly based on comparatively economic and relative effectively biological process, but owing to the water quality and quantity of this kind waste water is complicated and changeable, the refining plant processing efficiency is lower, the working cost costliness.Particularly in recent years, along with increasing of softening agent kind, various novel macromolecule raw materials, tensio-active agent and auxiliary agent etc. enter into factory effluent, cause waste water that higher toxicity is arranged, the biodegradability of waste water obviously reduces, intractability and expense further strengthen, and treat effluent often can not qualified discharge.Therefore, conventional processes is undergone technological transformation and reforms, and improve waste water treatment efficiency, reduce cost for wastewater treatment, guarantee effluent quality up to standard become plasticizer waste water handle in a difficult problem that needs to be resolved hurrily.
(publication number: CN1271692), mainly be made up of anaerobism part and aerobic part, flow process comprises anaerobic reactor, sewage backflow jar, aerobe selector switch, aeration tank, mudpan and mud acidification pool to a kind of process for treating high-concentration sewage.
A kind of treatment process (publication number: CN1611457) of high concentrated organic wastewater, this method is a core with anaerobic biofilter-Fenton reagent oxidation-contact oxidation method (A-F-O method), high concentrated organic wastewater is regulated after the pH, feed anaerobic biofilter (AF) bottom, and enter Fenton reagent oxidation reactor from the overflow of AF top, enter the neutralization precipitation pond after reaction for some time, remove Fe remaining in the waste water
2+After, enter contact oxidation reaction system, control certain residence time, through the second pond water outlet.
Existing treatment process mainly is that unified collection of various Chemical Manufacture waste water handled, the operating load and the processing costs of sewage treatment facility have so not only been increased, but also wasted a large amount of callable resources in the waste water, and the effluent quality after handling is difficult to up to standard.
Summary of the invention
The objective of the invention is to: provide a kind of categorised collection processing of plasticizer waste water and the system process of comprehensive utilization, this art breading stable effluent quality, but qualified discharge.Can be back to production after the purification of waste water, not influence the softening agent quality product, and investment and working cost economical rationality, the technology practical.
The general planning that the present invention proposes is: high-COD waste water and low COD waste water are separately handled.High-COD waste water is handled back up to standard discharging, and major part is back to production after the low COD wastewater treatment, and small portion is taken over discharging.
For high-COD waste water (COD6000～30000mg/L, BOD2000～10000mg/L, pH4～12), comprise DOG waste water, epoxy ester alkali cleaning waste water, oil and fat refining waste water and TOTM waste water, after DOG waste water, epoxy ester alkali cleaning waste water and oil and fat refining waste water carried out pre-treatment respectively, be mixed into biochemical system with TOTM waste water and handle.
For low COD waste water (COD500～2000mg/L, pH4～12), the laggard oxygen biological treatment of acting charitably of unified collection after coagulating sedimentation filters, by embrane method and catalytic ozonation advanced treatment, is back to production.
Technical process of the present invention may further comprise the steps:
To high-COD waste water:
(1) (COD8000～15000mg/L) enter oil trap removes degrease by adding sulfuric acid (or hydrochloric acid) breakdown of emulsion and oil removal to oil and fat refining waste water, and clear liquid enters neutralization tank after the filter bed dephosphorization;
(2) (COD30000～40000mg/L) enter oil trap removes degrease by adding sulfuric acid (or hydrochloric acid) breakdown of emulsion and oil removal to DOG waste water, and clear liquid enters neutralization tank after the detoxification decolouring is handled;
(3) (COD15000～25000mg/L) enter oil trap removes degrease by adding sulfuric acid (or hydrochloric acid) breakdown of emulsion and oil removal to epoxy ester alkali cleaning waste water, and clear liquid enters neutralization tank;
(4) three strands of waste water neutralization tank through massfraction be in 10～15% the alkali lye and after, with TOTM waste water (COD3000～10000mg/L) at equalizing tank mixing homogeneous;
(5) mixing water enters the anaerobic reactor anaerobic treatment, and the biogas of generation is stored in the gas holder comprehensive utilization;
(6) high loading biological tank aerobic treatment is advanced in the anaerobism water outlet, and water outlet is handled through hold concurrently oxygen-aerobe of settling tank post precipitation, after coagulating sedimentation is handled the back discharging;
(7) mud in each reaction unit regularly enters sludge sump, and filter is done, and filtrate enters the equalizing tank described in the step (4) by the waste liquid return-flow system and handles.
To hanging down COD waste water:
(1) unification of each strand waste water is collected in equalizing tank mixing homogeneous;
(2) the equalizing tank water outlet enters the processing of aerobe treating pond, can adopt technologies such as microbial film, aerobic contact oxidation, aerobic biofilter, conventional activated sludge process.
(3) the Aerobic Pond water outlet is further adopted the embrane method advanced treatment after coagulating sedimentation filters.
(4) the dense water of handling through the film equalizing tank that returns high-COD waste water is handled again, and fresh water is by the catalytic ozonation decolouring with production reuse after further removing micropollutant.
(5) mud in each reaction unit regularly enters sludge sump, and filter is done, and filtrate is handled by the equalizing tank that the waste liquid return-flow system enters high-COD waste water again.
Can produce a certain amount of waste water and gas in the whole process treatment process, wherein the waste oil reclaiming is produced, biogas fully utilizes behind desulfurizing and purifying, and the filtrate of sludge drying bed can be back to the high-concentration waste water equalizing tank by the waste liquid return-flow system, and the mud after filter is done can be used as paves the way or brickmaking etc.Accompanying drawing 1 is seen in technical process of the present invention.
In the oil trap described in the high-COD waste water treatment step (1,2,3), built-in swash plate, oil removal groove and weir plate, and be equipped with devices such as water distributor, aerator, automatic level controller (water pump and volume pump interlock control), recovery oil drum, pump.
Filter bed filler described in the step (1) can adopt CaCO
3, CaO etc., and should be equipped with the back flushing loop.
Detoxification decolouring described in the step (2) is handled, and can adopt Fe-C or ozonation technology.Fe-C technology mainly is to utilize little electrolytic action of Fe-C to reduce waste water COD, and improves the biodegradability of waste water; Ozone process mainly utilizes its OH free radical that decomposes generation to have extremely strong oxidation susceptibility, destroy to be difficult for biodegradable macromole phenyl ring type organic, and decolorizing effect is remarkable.This device will carry out antiseepage, the inwall epoxy anticorrosion is handled.
The described anaerobic reactor of step (5) can adopt UASB, EGSB, AF etc., and this device should be equipped with corresponding triphase separator, water distributor, filler, recycle pump, and encapsulation process.
The described mud filter of step (7) dry systems can directly be provided with sludge drying bed, and be equipped with the pressure filter auxiliary treatment, lays the perforation rising pipe all around, and gravel packing is laid in the bottom, and ground need be done antiseepage and be handled.Filtrate passes back into the high-concentration waste water equalizing tank by the waste liquid return-flow system, and the back outward transport is done in the mud filter.
Irritate in the filter described in the low COD wastewater treatment step (3), inner filling filtering material as fibrous bundle, fibrous nodules, ultra-filtration membrane, micro-filtrate, sandstone and filter core etc., and is equipped with back-purge system; Embrane method can adopt nanofiltration (NF), micro-filtration (UF), ultrafiltration (MF), reverse osmosis (RO) etc.
Catalytic ozonation in the step (4) is handled and is adopted copper sulfate or manganous sulfate as catalyzer, can adopt the homogeneous phase of catalysis concentration 5～8mg/L to handle, or 0.2～5% catalyzer is immobilized at γ-Al
2O
3On.
Technical essential of the present invention is as follows:
One, control automatically
1, fluid level controller: the automatic water outlet of fluid level controller is adopted in the oil trap draining, prevents waste water outflow in the pond when guaranteeing enough hydraulic detention times.
2, automatic intermittent aeration: oil trap and high loading aerobe pond aerating apparatus preparation automatic control system, the intermittent aeration of oil trap guarantees oil removal efficient, and reduces energy consumption.The intermittent aeration in high loading aerobe pond guarantees an amount of dissolved oxygen.
3, automatic medicament feeding system: settling tank and line mixer all adopt quantitative dosing coagulant of volume pump and precipitation agent, make added amount of chemical and wastewater treatment capacity be complementary, and guarantee treatment effect and save dosing.
Two, craft feature
1, the shunting of removing contamination: high-COD waste water and low COD waste water separate treatment, not only can reclaim useful resource in the waste water to greatest extent, and give full play to the function of each reactor, and the cost of water reuse in making reduces greatly.
2, classification pre-treatment: because high-COD waste water source is more, the ingredient difference, the useful resources in the per share waste water can be fully reclaimed in pre-treatment respectively, and pre-treatment can reduce the COD about 30%, has reduced the load of follow-up Biochemistry Reaction System.The detoxifcation decolorizing effect of Fe-C or ozone process has reduced the toxic action of DOG waste water to biochemical system.
3, multistage anaerobic-aerobic biochemical system: the one-level anaerobic reactor can adopt UASB, IC, EGSB, AF or anaerobic biofilter etc.Though the COD removal effect of anaerobic reactor is not high, it need not aeration, the mud generation is little, mud is difficult for expanding, anti impulsion load improves plurality of advantages such as B/C by force and fully, has improved waste water quality greatly, has reduced secondary pollution; The one-level aerobic reactor can adopt aerobic biofilter, high loading reaction tank, microbial film (MBR) reactor etc., and it can reduce in the waste water by about 60% COD to organic strong degradation capability; The secondary biochemical system can adopt A/O, A
2Reaction tanks such as/O, the difficult organism in further hydrolysis, the degrading waste water.
4, catalytic ozonation: catalytic ozonation can many-sidedly be removed and pollute, and effectively improves water quality.Since ozone can oxygenolysis in the water various impurity comprise the organism of colour developing, therefore can remove impurity caused in the water look effectively, smell, distinguish the flavor of, its decolouring and to improve the effect of micropollutant water remarkable.
Advantage of the present invention and application prospect:
Because water reclamation rate higher (＞50%) can be alleviated the demand pressure of chemical industrial plasticizer enterprise to water resources greatly, reduce the consumption of water resources.
Technology structures facility of the present invention is simpler, invests the working cost less expensive, both can be used as the newly-built sewage treatment facility of chemical enterprise, also can be used for the transformation of existing chemical enterprise sewage treatment facility.Reuse water can be back to production link, and to the not influence of quality of softening agent product, and water recovery economic benefit is big.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Fig. 2 is a COD change curve in the epoxy ester alkali cleaning waste water acid out process.
Embodiment
The invention will be further described below in conjunction with drawings and Examples.
1, high-COD waste water
Implementation step one: breakdown of emulsion oil removal pre-treatment
Get epoxy ester alkali cleaning waste water 2L (water quality: COD16000～25000mg/L, pH8～10), violent stirring slowly adds the vitriol oil, measures acidity in real time with pH meter, and sampling and measuring COD (through filter paper filtering) finishes to pH=1.5 under different pH.
Experimental result shows: in the process of pH=2.5～3, the COD value of water sample drops sharply to 12000～13000mg/L from 18000～25000mg/L, clearance＞33%, and when pH＜2.5, COD is difficult to further decline.
Through check, the oil and fat refining waste water quality is similar to epoxy ester alkali cleaning waste water quality, and the acid out effect is identical, and can adopt uses the same method carries out the acid out pre-treatment, because oil and fat refining waste water contains Phosphorus material, so the acid out water outlet is through CaCO
3Filter bed dephosphorization and neutralizing treatment.DOG waste water is after identical acid out process, because it contains difficult degradation toxic substances such as macromole phenyl ring class formation, so handle and raising B/C through the detoxifcation of Fe-C pond.
Implementation step two: neutralization is regulated
Above-mentioned pretreated several strands of waste water mix at equalizing tank with TOTM waste water, and lye pH adjustment are between 6.5～7.5 through preliminary sedimentation tank coagulation-post precipitation.
Implementation step three: the UASB anaerobic biological is handled
This reactor control hydraulic detention time HRT=48h, sludge seeding amount 10～15gVSS/L, pH=6.5～7.5, initial start control volumetric loading is at 0.5～1.0kgCOD/ (m
3D), i.e. UASB water inlet COD is controlled at 1500～2000mg/L.When water outlet COD clearance reaches 50% when above, press 0.5kgCOD/ (m
3D) amount increases load, intakes at full capacity until reactor.Stable back UASB water outlet COD is about 5000mg/L.
Implementation step four: high loading activated sludge tank
The UASB water outlet enters the high loading activated sludge tank, this section control hydraulic detention time HRT=24h, sludge concentration MLSS4000～5000mg/L, pH=6.5～7.5, fully aeration and stirring.After this reactor stable water outlet, COD can be controlled at about 2000mg/L.
Implementation step five: the A/O oxygen-aerobic biochemical pond of holding concurrently
Control A section: hydraulic detention time HRT=1～3h, sludge concentration MLSS=2000～2500mg/L, pH=6～8; O section: hydraulic detention time HRT=24～36h, sludge concentration MLSS=2000～2500mg/L, pH=6～8.Water inlet COD=2000～2500mg/L, stable water outlet is at COD550～650mg/L.
Implementation step six: coagulation-precipitation process
Coagulating agent: adopt PAC (polymerize aluminum chloride) or PAM (polyacrylamide).
Water source: A/O biochemistry pool water outlet.
Get 500ml waste water in the 1000mg beaker, under about 150r/min, stir fast, add a certain amount of coagulant solution of concentration known, continue to stir fast 3min, stirring velocity is turned down to 50r/min, stir 10min at a slow speed; Leave standstill 30min, draw supernatant liquor as solution to be measured with 50ml syringe 0.5cm place under liquid level then.
Experimental results show that: after 200～600mg/L coagulating agent coagulation-precipitation process, water outlet COD reduces to below the 450mg/L, reaches " integrated wastewater discharge standard " three grades of emission standards in (GB8978-1996).
2, low COD waste water
Implementation step one: neutralization is regulated
Collect each low COD waste water, comprise vacuum pump waste water (COD800～2000mg/L, pH4～10), water-ring pump waste water (300～1000mg/L, pH4～10) and water coolant (300～1000mg/L, pH4～10) in equalizing tank, evenly after the water quality, regulating waste water ph is 6～8.
Implementation step two: aerobe is handled
Fresh water enters activated sludge tank and carries out aerobic treatment, control hydraulic detention time HRT=8～10h, and sludge concentration MLSS=2000～3000mg/L, pH=6～8, COD is at 700～1000mg/L in water inlet, and water outlet COD is stabilized in 350～450mg/L.
Implementation step three: coagulation-precipitation-filtration
Coagulating agent: adopt PAC (polymerize aluminum chloride) or PAM (polyacrylamide).
Water source: aerobe pond water outlet.
Get 300ml waste water in the 1000mg beaker, under about 150r/min, stir fast, add a certain amount of coagulant solution of concentration known, continue to stir fast 3min, stirring velocity is turned down to 50r/min, stir 10min at a slow speed; Leave standstill 30min, draw supernatant liquor with 50ml syringe 0.5cm place under liquid level then, after filtering as solution to be measured.
Experimental results show that: after 300～500mg/L coagulating agent coagulation-precipitation-filtration treatment, water outlet COD reduces to below the 300mg/L, far reaches " integrated wastewater discharge standard " three grades of emission standards in (GB8978-1996).
Implementation step four: nanofiltration (NF) film is handled
With 1 ton of uniform mixing water after filtration precision be 1～10 micron honeycomb filter element filtering, be the reverse osmosis equipment of 5t/h with the flooding velocity that the U.S. DesalDL of GE company rolling nanofiltration membrane is installed, under the 0.7Mpa condition, handle obtaining dense water and fresh water.0.65～0.9 ton of the fresh water that the nanofiltration operation is discharged, 0.1～0.35 ton in the dense water of discharge.After measured, fresh water COD is between 80～150mg/L.
Implementation step five: catalytic ozonation is handled
Catalyzer: adopt copper sulfate or manganous sulfate.
Water source: nanofiltration water outlet.
In the bubbling reactor of 5L, add catalyzer 5～8mg, control ozone dosage 50～120mg/L, hydraulic detention time HRT10～30min, COD reduces to 60mg/L by the preceding 100mg/L of reaction, and colourity is reduced to 0 times.
Complete process embodiment: the 750t/d chemical industrial plasticizer waste water is handled and reuse project, and accompanying drawing 1 is seen in the present embodiment technical process.
1, technical process
Certain 750t/d chemical industrial plasticizer waste water processing and reuse project are as shown in Figure 1.
2, high-COD waste water
2.1 breakdown of emulsion oil removal pre-treatment
The oil and fat refining waste water of the high COD of 50t/d is arrived oil trap with pump delivery, in oil trap, add sulfuric acid, regulate about pH value to 3, simultaneously to carrying out an amount of aeration in the pond, through breakdown of emulsion, there is the oil in water emulsion that is suspension in a large number to separate out, and is collected in the waste water surface, intercept in the oil removal groove through weir plate, flow into along oil exit pipe and reclaim oil drum.Subnatant to the lime carbonate filter bed and after the dephosphorization, flows into neutralization tank through lift pump certainly:
The DOG waste water of the high COD of 10t/d is arrived oil trap with pump delivery, in oil trap, add sulfuric acid, regulate about pH value to 3, simultaneously to carrying out an amount of aeration in the pond, through breakdown of emulsion, there is the oil in water emulsion that is suspension in a large number to separate out, and is collected in the waste water surface, intercept in the oil removal groove through weir plate, flow into along oil exit pipe and reclaim oil drum.Subnatant flows into neutralization tank after entering Fe-C pond detoxification treatment certainly;
The epoxy ester alkali cleaning waste water of the high COD of 25t/d is arrived oil trap with pump delivery, in oil trap, add sulfuric acid, regulate about pH value to 3, simultaneously to carrying out an amount of aeration in the pond, through breakdown of emulsion, there is the oil in water emulsion that is suspension in a large number to separate out, and is collected in the waste water surface, intercept in the oil removal groove through weir plate, flow into along oil exit pipe and reclaim oil drum.Subnatant is from flowing into neutralization tank.
The adjusting 2.2 catchment
Because waste disposal plant all is according to certain water quality and water yield standard design, require water inlet evenly.In order to guarantee the steady running of sewage treatment facility, reduce the disadvantageous effect of impact load to processing unit, establish an equalizing tank, carry out water yield equilibrium and water quality regulation to advancing biochemical system sewage.The TOTM waste water of 25t/d directly is delivered to this equalizing tank through pump, comes water to mix with the neutralization precipitation pond.
2.3 the bio combined processing of anaerobic-aerobic
Owing to contain a large amount of raw materials and processing intermediate product in the chemical industrial plasticizer waste water, make that the pH of waste water and COD are all higher.The main effect of anaerobic acidification hydrolysis treatment be with macromole, difficult for biological degradation or insoluble solid thing be decomposed into small molecules, can biochemical organism, improve the biodegradability of waste water.
The main effect of aerobic treatment is to remove remaining most of organism, and the COD of sewage concentration after anaerobic treatment is still higher, is difficult to reach the sewage discharge requirement, so aerobic section still needs than long residence time.
This technology is in conjunction with COD concentration height in the chemical industrial plasticizer waste water, and the characteristics that the hazardous and noxious substances kind is many adopt the Two-Stage Biochemical treatment system in UASB+ high loading biological tank+A/O pond.
2.4 materialization is handled
Must carry out coagulation-precipitation process after the biological treatment,, guarantee to reach the sewage discharge requirement with further removal suspended state material and COD.
3, low COD waste water
The adjusting 3.1 catchment
Respectively the vacuum pump waste water of 420t/d, the water-ring pump waste water of 85t/d, the water coolant of 135t/d are carried out water quality regulation and water yield equilibrium with pump delivery to equalizing tank.
3.2 aerobe is handled
Because the COD concentration of this part waste water is lower, and macromole difficult degradation and hazardous and noxious substances are less, handle so can directly carry out aerobe.
3.3 materialization is handled
Water outlet can be satisfied " integrated wastewater discharge standard " three grades of emission standards in (GB8978-1996) after coagulation-precipitation-filtration is handled again.
3.4 nanofiltration (NF) film is handled
The intimate mixing water of 640t/d is handled with the nanofiltration desalter that pump enters 30t/h, and 450t/d fresh water enters follow-up catalytic ozonation and handles, and the dense water of 190t/d enters the equalizing tank 1 of high-COD waste water treatment system and handles.
3.5 catalytic ozonation
Catalytic ozonation can many-sidedly be removed and pollute, and effectively improves water quality.Since ozone can oxygenolysis in the water various impurity comprise the organism of colour developing, therefore can effectively remove impurity caused in the water look, smell, distinguish the flavor of, its decolouring and to improve the effect of micropollutant water remarkable.This process can be removed the COD of the colourity more than 90% in the water and 50%～80%.
4, each structures processing efficiency and effluent quality
Each structures processing efficiency and effluent quality see table 1 for details.
Table 1 each structures processing efficiency and effluent quality
| Processing unit | COD Cr | BOD 5 | |||||
| Water inlet (mg/L) | Water outlet (mg/L) | Clearance (%) | Water inlet (mg/L) | Water outlet (mg/L) | Clearance (%) | ||
| The high concentration water handles | The oil removal breakdown of emulsion | 13000 | 8650 | 33 | 4300 | 3940 | 8 |
| The UASB reactor | 8650 | 3030 | 65 | 3940 | 1182 | 70 | |
| The high loading oxidation pond | 3030 | 1500 | 50 | 1182 | 472 | 60 | |
| The A/O pond | 1500 | 450 | 70 | 472 | 100 | 78 | |
| Low concentration of water is handled | Aerobic Pond | 700 | 350 | 50 | 250 | 100 | 60 |
| Coagulating sedimentation filters | 350 | 250 | 28.6％ | / | / | / | |
| Nanofiltration (NF) | 250 | 100 | 66.7％ | / | / | / | |
| Ozone oxidation | 100 | 40 | 60％ | / | / | ||
| Standard value | ＜500 | ＜300 | |||||
5, working cost
The expense of handling high-concentration waste water is 5.82 yuan/ton; When disregarding water reuse economic benefit, the expense of handling low concentration wastewater is 1.38 yuan/ton.In addition, project will produce 312m
3/ d biogas is recycled behind gas holder storage and dry desulfurization.
Claims (9)
1. the process for reclaiming of chemical industrial plasticizer waste water, described chemical industrial plasticizer waste water comprises the oil and fat refining waste water of COD8000～15000mg/L, the DOG waste water of COD30000～40000mg/L, the epoxy ester alkali cleaning waste water of COD15000～25000mg/L, TOTM waste water and the low COD waste water of COD3000～10000mg/L, it is characterized in that following steps:
(1) oil and fat refining waste water enters oil trap, removes degrease by adding sulfuric acid or salt naphtenic acid and oil removal, and clear liquid enters neutralization tank after the filter bed dephosphorization;
(2) DOG waste water enters oil trap, removes degrease by adding sulfuric acid or salt naphtenic acid and oil removal, and clear liquid enters neutralization tank after the detoxification decolouring is handled;
(3) epoxy ester alkali cleaning waste water enters oil trap, removes degrease by adding sulfuric acid or salt naphtenic acid and oil removal, and clear liquid directly enters neutralization tank;
(4) three strands of waste water neutralization tank through massfraction be in 10～15% the alkali lye and after, with TOTM waste water at equalizing tank mixing homogeneous;
(5) mixing water behind the homogeneous enters the anaerobic reactor anaerobic treatment, and the biogas of generation is stored in the gas holder comprehensive utilization;
(6) the anaerobism water outlet is entered high loading aerobe pond and is handled, and water outlet is handled through the settling tank post precipitation oxygen-aerobe of holding concurrently, after coagulating sedimentation handle the back and discharge;
(7) mud in each reaction unit regularly enters sludge sump, and filter is done, and filtrate enters the described equalizing tank of step (4) by the waste liquid return-flow system and handles;
(8) will hang down the unification of COD waste water and be collected in equalizing tank mixing homogeneous;
(9) the equalizing tank water outlet enters the aerobe treating pond and handles selection microbial film, aerobic contact oxidation, aerobic biofilter, conventional activated sludge process technology one.
(10) the Aerobic Pond water outlet is further adopted the embrane method advanced treatment after coagulating sedimentation filters;
(11) the dense water of handling through film returns the described equalizing tank of step (4) and handles, and fresh water is by the catalytic ozonation decolouring with production reuse after further removing micropollutant;
(12) mud in each reaction unit regularly enters sludge sump, and filter is done, and filtrate enters the described equalizing tank of step (4) by the waste liquid return-flow system and handles.
(13) waste oil reclaiming in the above step is produced, biogas fully utilizes behind desulfurizing and purifying, and the filtrate of sludge drying bed is back to equalizing tank by the waste liquid return-flow system, and the mud after filter is done is as paving the way or brickmaking.
2. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the oil trap described in the step (1,2,3), built-in swash plate, oil removal groove and weir plate, and be equipped with water distributor, aerator, contain automatic level controller, recovery oil drum and the pump of water pump and volume pump interlock control.
3. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the filler of filter bed described in the step (1) adopts CaCO
3, CaO, and be equipped with the back flushing loop.
4. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the detoxification decolouring described in the step (2) is handled and is adopted Fe-C or ozonation technology.
5. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the described anaerobic reactor of step (5) adopts UASB, EGSB, AF, and be equipped with corresponding triphase separator, water distributor, filler, recycle pump, and encapsulation process.
6. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the described mud filter of step (7) dry systems directly is provided with sludge drying bed, and outfit pressure filter, lay the perforation rising pipe, gravel packing is laid in the bottom, and ground is done antiseepage and handled.
7. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the described filter of step (8) is irritated, inner filling fiber bundle, fibrous nodules, ultra-filtration membrane, micro-filtrate, sandstone and filter element filtering material one, and be equipped with back-purge system;
8. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the described embrane method of step (10) adopts nanofiltration (NF), micro-filtration (UF), ultrafiltration (MF), reverse osmosis (RO) one.
9. according to the process for reclaiming of the described chemical industrial plasticizer waste water of claim 1, it is characterized in that: the catalytic ozonation in the step (11) is handled and is adopted copper sulfate or manganous sulfate as catalyzer, catalysis concentration is that the homogeneous phase of 5～8mg/L is handled, or 0.2～5% catalyzer is immobilized at γ-Al
2O
3On.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2008100596476A CN100545112C (en) | 2008-02-01 | 2008-02-01 | The process for reclaiming of chemical industrial plasticizer waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2008100596476A CN100545112C (en) | 2008-02-01 | 2008-02-01 | The process for reclaiming of chemical industrial plasticizer waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101224937A true CN101224937A (en) | 2008-07-23 |
| CN100545112C CN100545112C (en) | 2009-09-30 |
Family
ID=39857178
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2008100596476A Active CN100545112C (en) | 2008-02-01 | 2008-02-01 | The process for reclaiming of chemical industrial plasticizer waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100545112C (en) |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102070238A (en) * | 2011-02-25 | 2011-05-25 | 中国海洋石油总公司 | Process method for treating reverse osmosis concentrated water in refining waste water by ozone catalytic oxidization |
| CN102153171A (en) * | 2011-05-26 | 2011-08-17 | 中国海洋石油总公司 | Combined method for treating refinery wastewater by adopting reverse osmosis and catalytic ozonation |
| CN102531283A (en) * | 2011-12-30 | 2012-07-04 | 南昌大学 | Method for treating food processing organic wastewater containing high-concentration fat and suspended matter |
| CN102583889A (en) * | 2012-02-24 | 2012-07-18 | 美景（北京）环保科技有限公司 | Wastewater treatment method and wastewater treatment system |
| CN103011519A (en) * | 2012-12-24 | 2013-04-03 | 绍兴县江滨水处理有限公司 | Treatment method and equipment for high-salt and alkali-weight-reduction waste water |
| CN103739120A (en) * | 2014-01-10 | 2014-04-23 | 天津市环境保护科学研究院 | Coupling type membrane ozone catalytic reaction system and device for treating organic wastewater |
| CN104591511A (en) * | 2015-02-15 | 2015-05-06 | 富阳鸿祥技术服务有限公司 | Treatment method for industrial oily wastewater |
| CN104609673A (en) * | 2015-02-03 | 2015-05-13 | 厦门科林尔环保科技有限公司 | Non-antibiotic pharmaceutical wastewater treatment process |
| CN104609666A (en) * | 2015-01-21 | 2015-05-13 | 梁亨 | Treatment method for liquid waste from production of plasticizer for chemical industry |
| CN104609674A (en) * | 2015-02-15 | 2015-05-13 | 富阳鸿祥技术服务有限公司 | Treatment system for industrial oily wastewater |
| CN104803542A (en) * | 2014-01-26 | 2015-07-29 | 北京林业大学 | Integrated treatment and reuse technology of esterification wastewater |
| CN104891701A (en) * | 2014-03-05 | 2015-09-09 | 天津福润龙科技发展有限公司 | Wastewater purification apparatus and wastewater treatment process |
| CN106396294A (en) * | 2016-12-06 | 2017-02-15 | 大同新成新材料股份有限公司 | Treatment method of lithium battery electrolyte cask washing wastewater |
| GB2565762A (en) * | 2017-08-04 | 2019-02-27 | Prosper Env Tech Enterprise Co Ltd | Method and apparatus for reducing secondary pollution and recovering water from dyeing and finishing wastewater for reuse |
| CN111072217A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Method for advanced treatment and recycling of saliferous oil refining wastewater |
| CN112607962A (en) * | 2020-12-04 | 2021-04-06 | 上海天汉环境资源有限公司 | Emulsion wastewater treatment method and system |
| CN112624426A (en) * | 2020-12-30 | 2021-04-09 | 河南庆安化工高科技股份有限公司 | Plasticizer VOCSWastewater treatment process |
| CN113443750A (en) * | 2021-07-29 | 2021-09-28 | 南通海珥玛科技股份有限公司 | Experimental method for treating esterification reaction wastewater |
-
2008
- 2008-02-01 CN CNB2008100596476A patent/CN100545112C/en active Active
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102070238A (en) * | 2011-02-25 | 2011-05-25 | 中国海洋石油总公司 | Process method for treating reverse osmosis concentrated water in refining waste water by ozone catalytic oxidization |
| CN102153171A (en) * | 2011-05-26 | 2011-08-17 | 中国海洋石油总公司 | Combined method for treating refinery wastewater by adopting reverse osmosis and catalytic ozonation |
| CN102531283A (en) * | 2011-12-30 | 2012-07-04 | 南昌大学 | Method for treating food processing organic wastewater containing high-concentration fat and suspended matter |
| CN102583889A (en) * | 2012-02-24 | 2012-07-18 | 美景（北京）环保科技有限公司 | Wastewater treatment method and wastewater treatment system |
| CN103011519A (en) * | 2012-12-24 | 2013-04-03 | 绍兴县江滨水处理有限公司 | Treatment method and equipment for high-salt and alkali-weight-reduction waste water |
| CN103739120A (en) * | 2014-01-10 | 2014-04-23 | 天津市环境保护科学研究院 | Coupling type membrane ozone catalytic reaction system and device for treating organic wastewater |
| CN103739120B (en) * | 2014-01-10 | 2014-11-26 | 天津市环境保护科学研究院 | Coupling type membrane ozone catalytic reaction system and device for treating organic wastewater |
| CN104803542A (en) * | 2014-01-26 | 2015-07-29 | 北京林业大学 | Integrated treatment and reuse technology of esterification wastewater |
| CN104891701A (en) * | 2014-03-05 | 2015-09-09 | 天津福润龙科技发展有限公司 | Wastewater purification apparatus and wastewater treatment process |
| CN104609666A (en) * | 2015-01-21 | 2015-05-13 | 梁亨 | Treatment method for liquid waste from production of plasticizer for chemical industry |
| CN104609673A (en) * | 2015-02-03 | 2015-05-13 | 厦门科林尔环保科技有限公司 | Non-antibiotic pharmaceutical wastewater treatment process |
| CN104609674A (en) * | 2015-02-15 | 2015-05-13 | 富阳鸿祥技术服务有限公司 | Treatment system for industrial oily wastewater |
| CN104591511A (en) * | 2015-02-15 | 2015-05-06 | 富阳鸿祥技术服务有限公司 | Treatment method for industrial oily wastewater |
| CN104609674B (en) * | 2015-02-15 | 2016-04-06 | 富阳鸿祥技术服务有限公司 | A kind for the treatment of system of industrial oily waste water |
| CN104591511B (en) * | 2015-02-15 | 2016-04-06 | 富阳鸿祥技术服务有限公司 | A kind for the treatment of process of industrial oily waste water |
| CN106396294A (en) * | 2016-12-06 | 2017-02-15 | 大同新成新材料股份有限公司 | Treatment method of lithium battery electrolyte cask washing wastewater |
| GB2565762A (en) * | 2017-08-04 | 2019-02-27 | Prosper Env Tech Enterprise Co Ltd | Method and apparatus for reducing secondary pollution and recovering water from dyeing and finishing wastewater for reuse |
| GB2565762B (en) * | 2017-08-04 | 2022-02-16 | Prosper Env Tech Enterprise Co Ltd | Method and apparatus for reducing secondary pollution and recovering water from dyeing and finishing wastewater for reuse |
| CN111072217A (en) * | 2018-10-22 | 2020-04-28 | 中国石油化工股份有限公司 | Method for advanced treatment and recycling of saliferous oil refining wastewater |
| CN112607962A (en) * | 2020-12-04 | 2021-04-06 | 上海天汉环境资源有限公司 | Emulsion wastewater treatment method and system |
| CN112624426A (en) * | 2020-12-30 | 2021-04-09 | 河南庆安化工高科技股份有限公司 | Plasticizer VOCSWastewater treatment process |
| CN113443750A (en) * | 2021-07-29 | 2021-09-28 | 南通海珥玛科技股份有限公司 | Experimental method for treating esterification reaction wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100545112C (en) | 2009-09-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100545112C (en) | The process for reclaiming of chemical industrial plasticizer waste water | |
| CN102659283B (en) | Process for treating and recovering dye industrial wastewater | |
| CN101074141B (en) | Process for regenerating, recovering and reutilizing low-concentration organic waste water | |
| CN1765779A (en) | Printing and dyeing wastewater recovery and disposal method | |
| CN105693014A (en) | Sewage treatment system and sewage treatment method | |
| CN103435233B (en) | Equipment and method for recycling chemical fiber continuous-spinning wastewater | |
| CN103159381A (en) | Fine chemical wastewater treatment and reuse method | |
| CN102139991A (en) | Method for treating and recycling coal-derived natural gas waste water and device thereof | |
| CN102557359A (en) | Device for treating wastewater during production of pentaerythritol | |
| CN105565581B (en) | Coal ethylene wastewater integrated conduct method | |
| CN104118973A (en) | Technique for processing reverse osmosis concentrated water | |
| CN100591632C (en) | Advanced treatment method and device for dyeing waste water by ozone iron zinc catalysis | |
| CN105060636A (en) | System and technology for reuse of printing and dyeing wastewater reclaimed water subjected to quality-based treatment | |
| CN207062081U (en) | A kind of pharmaceutical wastewater processing system | |
| CN105984992A (en) | Paint wastewater treatment method | |
| CN201598224U (en) | Biological nitrogen and phosphorus removal treatment and filter integrated sewage treatment system | |
| CN104386881B (en) | A kind of Coal Chemical Industry production wastewater treatment and high power reuse technology and dedicated system thereof | |
| CN209098459U (en) | A kind of high gravity fermentation class antibiotic waste water processing system | |
| CN203200124U (en) | High-efficiency treatment and comprehensive recycling device for waste paper papermaking waste water | |
| CN106430846A (en) | Efficient treatment integrated process for recalcitrant wastewater with low organic matter content | |
| CN214299762U (en) | Polyester fiber waste water reuse of reclaimed water device | |
| CN205328795U (en) | Wet spinning acrylic fibres production polymerization effluent disposal system | |
| CN105461163B (en) | Wet spinning acrylic produces polymeric wastewater processing system and processing method | |
| CN114149140A (en) | Caprolactam production wastewater treatment method | |
| CN113264638A (en) | Landfill leachate treatment system and technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |