CN104230032B - A kind of Zero-discharge coked wastewater treatment system - Google Patents

A kind of Zero-discharge coked wastewater treatment system Download PDF

Info

Publication number
CN104230032B
CN104230032B CN201310230195.4A CN201310230195A CN104230032B CN 104230032 B CN104230032 B CN 104230032B CN 201310230195 A CN201310230195 A CN 201310230195A CN 104230032 B CN104230032 B CN 104230032B
Authority
CN
China
Prior art keywords
reverse osmosis
ro reverse
cross
flow
filter
Prior art date
Application number
CN201310230195.4A
Other languages
Chinese (zh)
Other versions
CN104230032A (en
Inventor
王余标
Original Assignee
上海净意环保设备有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 上海净意环保设备有限公司 filed Critical 上海净意环保设备有限公司
Priority to CN201310230195.4A priority Critical patent/CN104230032B/en
Publication of CN104230032A publication Critical patent/CN104230032A/en
Application granted granted Critical
Publication of CN104230032B publication Critical patent/CN104230032B/en

Links

Abstract

The invention provides a kind of coking wastewater processing system, comprise two-stage precipitation outlet sump connected successively, preliminary sedimentation tank, cross-flow catalysis system, coagulative precipitation device, more medium filter, ultrafiltration cartridge filter, ultra-filtration equipment, ultrafiltration product pond, RO reverse osmosis cartridge filter, one-level RO reverse osmosis filter, secondary RO reverse osmosis filter.Coking wastewater processing system provided by the invention achieves the integrated of wastewater processing technology, and service efficiency is high, and water quality can reach the standard of water of productive use completely, and the demineralization due to cross-flow system realizes the zero release of internal recycle that salinity do not accumulate and coking chemical waste water.And the waste water of the dense water end (W.E.) of one-level RO reverse osmosis filter and secondary RO reverse osmosis filter enters cross-flow catalysis system by three-dimensional electrolysis oxidation reactor again except after salinity and organism, realizes the closed cycle of system, realizes zero environmental.

Description

A kind of Zero-discharge coked wastewater treatment system

Technical field

The present invention relates to a kind of Waste Water Treatment, particularly relate to a kind of coking wastewater processing system realizing zero release.

Background technology

Coking chemical waste water is mainly from the water of productive use in coke oven gas primary-cooling and coking production process and vapor condensation waste water.In coking chemical waste water, Pollutant levels are high, are difficult to degraded, due to the existence of nitrogen, cyanogen in coking chemical waste water, bring larger difficulty to process is up to standard; Wastewater discharge is large, and burnt water consumption per ton is greater than 2.5t; Waste water harm is large, and in coking chemical waste water, polycyclic aromatic hydrocarbons is not only difficult to degraded, and usual or strong carcinogen, also directly threatens human health while causing severe contamination to environment.

Coke-oven plant mainly produces the Chemicals such as coke, business coal gas, sulphur ammonium and light benzene.This factory coke tar recovery system adopts sulphur ammonium flow process, and tar production adopts the continuous still battery of tube furnace two tower, and industry how production technique is twin furnace double tower continuous still battery, washing, refining.In coke-oven gas cooling, washing, crude benzol processing and Process of Tar Processing, produce the trade effluent containing phenol, cyanogen, oil, ammonia and large amount of organic.

Therefore how waste water being carried out advanced treatment, has been a problem in the urgent need to address in present stage industrial production.

Summary of the invention

The object of this invention is to provide a kind of coking wastewater processing system, it can solve the above-mentioned shortcoming of prior art.

Technical scheme of the present invention is to provide a kind of coking wastewater processing system, comprises two-stage precipitation outlet sump connected successively, preliminary sedimentation tank, cross-flow catalysis system, coagulative precipitation device, more medium filter, ultrafiltration cartridge filter, ultra-filtration equipment, ultrafiltration product pond, RO reverse osmosis cartridge filter, one-level RO reverse osmosis filter, secondary RO reverse osmosis filter.

Preferably, described coking wastewater processing system also comprises three-dimensional electrolysis oxidation reactor, described one-level RO reverse osmosis filter is connected with three-dimensional electrolysis oxidation reactor with the dense water end (W.E.) of secondary RO reverse osmosis filter, and the outlet of described three-dimensional electrolysis oxidation reactor is connected with the import of cross-flow catalysis system.

Preferably, described coking wastewater processing system also comprises dense water collecting groove, the outlet of described ultra-filtration equipment is also connected with the import of dense water collecting groove, the outlet of described dense water collecting groove is connected with three-dimensional electrolysis oxidation reactor, and be connected with the import of the cross-flow catalysis system import of heterogeneous cross-flow catalysis system of the outlet of described three-dimensional electrolysis oxidation reactor is connected.

Preferably, described one-level RO reverse osmosis filter is connected with three-dimensional electrolysis oxidation reactor by dense water collecting groove with the dense water end (W.E.) of secondary RO reverse osmosis filter.

Preferably, described cross-flow catalysis system comprises the heterogeneous cross-flow catalytic unit of 1 heterogeneous cross-flow catalytic unit or multiple series connection.

Preferably, described cross-flow catalysis system comprises the heterogeneous cross-flow catalytic unit of 2 series connection, is followed successively by one-level heterogeneous cross-flow catalytic unit and the heterogeneous cross-flow catalytic unit of secondary.

Preferably, the water purification end of described one-level RO reverse osmosis filter and secondary RO reverse osmosis filter, the water purification end of secondary RO reverse osmosis filter is connected with production reclaiming system.

Preferably, the water purification end of secondary RO reverse osmosis filter is connected with discharge equipment.

Preferably, described preliminary sedimentation tank is made up of reactive tank, flocculation tank, settling bath.

Present invention also offers a kind of method adopting above-mentioned coking wastewater processing system Treatment of Wastewater in Coking, comprise the following steps:

Step 1, coking chemical waste water enters preliminary sedimentation tank by two-stage precipitation outlet sump, adds flocculation agent, through flocculation sediment, except the suspended substance defocused in waste water;

Step 2, the waste water after step 1 processes flows into cross-flow catalysis system, and add acid and oxygenant, degradable organic pollutant, then adjust ph is to 8-8.5;

Step 3, the waste water after step 2 processes flows in coagulative precipitation device, precipitation, and supernatant liquor, successively through more medium filter, removes colloidal particle, macromolecule organic;

Step 4, the supernatant liquor after step 3 processes, further through ultrafiltration cartridge filter and ultra-filtration equipment filtration treatment, flows into ultrafiltration and produces pond;

Step 5, the waste water after step 4 processes through one-level RO reverse osmosis filter, secondary RO reverse osmosis filter reverse-osmosis treated removing inorganic salt, organism, microorganism and colloid, is discharged after reaching emission standard successively.

Preferably, described method also comprises step 6: in step 5, one-level RO reverse osmosis filter and the dense water end (W.E.) waste water of secondary RO reverse osmosis filter enter three-dimensional electrolysis oxidation reactor, further except after freshen and organism, flow into cross-flow catalysis system, then repeating step 2,3,4 and 5.

Wherein, step 6 can repeatedly repeatedly.

Preferably, step 6 at least repeats once.

Preferably, oxygenant described in step 2 is hydrogen peroxide.

Coking wastewater processing system provided by the invention achieves the integrated of wastewater processing technology, service efficiency is high, water quality can reach the standard of water of productive use completely, demineralization due to cross-flow system realizes the zero release of internal recycle that salinity do not accumulate and coking chemical waste water, and the waste water of the dense water end (W.E.) of one-level RO reverse osmosis filter and secondary RO reverse osmosis filter enters cross-flow catalysis system by three-dimensional electrolysis oxidation reactor again except after salinity and organism, realize the closed cycle of system, realize zero environmental.

Accompanying drawing explanation

Fig. 1 is the structural representation of coking wastewater processing system described in embodiment;

Fig. 2 is Treatment of Coking Effluent schema.

Embodiment

With reference to the accompanying drawings, in conjunction with specific embodiments Ben Fanming is further described, to understand the present invention better.

As illustrated in fig. 1 and 2, a kind of coking wastewater processing system, comprises two-stage precipitation outlet sump 1, preliminary sedimentation tank 2, cross-flow catalysis system, coagulative precipitation device 5, more medium filter 6, ultrafiltration cartridge filter 7, ultra-filtration equipment 8, ultrafiltration product pond 9, RO reverse osmosis cartridge filter 10, one-level RO reverse osmosis filter 11, secondary RO reverse osmosis filter 12, dense water collecting device 13, discharge equipment 14 and three-dimensional electrolysis oxidation reactor 15; Wherein, described cross-flow catalysis system comprises the heterogeneous cross-flow catalytic unit of two series connection, is followed successively by one-level heterogeneous cross-flow catalytic unit 3 and the heterogeneous cross-flow catalytic unit 4 of secondary.

The outlet of two-stage precipitation outlet sump 1 connects preliminary sedimentation tank 2, the heterogeneous cross-flow catalytic unit 3 of one-level of the outlet connection of preliminary sedimentation tank 2, the outlet of one-level heterogeneous cross-flow catalytic unit 3 connects the heterogeneous cross-flow catalytic unit 4 of secondary, the outlet of the heterogeneous cross-flow catalytic unit 4 of secondary connects coagulative precipitation device 5, the outlet of coagulative precipitation device 5 connects more medium filter 6, the outlet of more medium filter 6 connects ultrafiltration cartridge filter 7, and the outlet of ultrafiltration cartridge filter 7 connects ultra-filtration equipment 8;

The outlet of ultra-filtration equipment 8 connects ultrafiltration and produces pond 9, the outlet that is produced from pond 9 in ultrafiltration connects RO reverse osmosis cartridge filter 10, the outlet of RO reverse osmosis cartridge filter 10 connects one-level RO reverse osmosis filter 11, the outlet of the water purification end of one-level RO reverse osmosis filter 11 connects the outlet connection discharge equipment 14 of secondary RO reverse osmosis filter 12, secondary RO reverse osmosis filter 12 water purification end.

The outlet of ultra-filtration equipment 8 also connects dense water collecting groove 13;

The dense water collecting groove 13 of all connections of the outlet of the dense water end (W.E.) of one-level RO reverse osmosis filter 11 and secondary RO reverse osmosis filter 12.

The outlet of dense water collecting groove 13 connects the import of three-dimensional electrolysis oxidation reactor 15, and three-dimensional electrolysis oxidation reactor 15 exports the import connecting the heterogeneous cross-flow catalytic unit 3 of one-level.

Two-stage precipitation outlet sump of the present invention water outlet, is promoted in the reactive tank of preliminary sedimentation tank by pump, removes the suspended substance of the overwhelming majority after adding flocculation agent coagulating sedimentation.Preliminary sedimentation tank water outlet, from flowing into the heterogeneous cross-flow catalysis system of one-level, adds acid, oxygenant simultaneously, from flowing into the heterogeneous cross-flow catalysis system of secondary after fully stirring.After one-level, the heterogeneous cross-flow catalytic treatment of secondary, the most organic pollutants mineralising in waste water is effectively decomposed, and is converted into harmless small molecules inorganics even up hill and dale, reduces the processing load of subsequent technique section.Waste water removes suspended substance in water and colloidalmaterial through more medium filter.Waste water through ultrafiltration system (ultrafiltration cartridge filter and ultra-filtration equipment) further turbidity removal and except degerming, virus and other objectionable impuritiess, for follow-up RO system provides guarantee water quality.Waste water, further across secondary RO system, ensures standard water discharge discharge.The waste water of the dense water end (W.E.) of RO system further except after freshen and organism through three-dimensional electrolysis oxidation reactor, again enters cross-flow catalysis system, realizes the closed cycle of system.

The preliminary sedimentation tank of this reality invention is made up of reactive tank, flocculation tank, settling bath, and waste water, by adding flocculation agent in reactive tank, enters settling bath after flocculation tank flocculation.This system effectively can remove the suspended substance in waste water, reduces the COD in waste water and salinity..

Heterogeneous cross-flow catalytic unit of the present invention, based on electrochemical techniques principle, utilizes the Strong oxdiative particle generated in catalytic reaction process, with the organic pollutant in waste water without selectively fast chain reaction occurring, carries out oxidative degradation.Heterogeneous cross-flow catalytic unit includes multiple filler, and filler contains iron-carbon, carbon, catalytic filler, softening filler etc.Obvious redox-potential is there is between FeC and Fe poor in waste water, countless multiple Wei battery is formed like this at Fe and FeC, Fe is anode, FeC is negative electrode, add macroscopic cathode material more in systems in which, namely during inertia charcoal (graphite, coke, gac, coal) particle, Fe contacts with charcoal, then form macroscopical battery.The comprehensive action of microbattery and macroscopical battery strengthens wastewater treatment usefulness.Heterogeneous cross-flow catalysis system is adjusted back groove by pH regulator groove, cross-flow catalytic reaction zone and pH and is formed, its operation scheme is as follows: when after the pH regulator groove that waste water enters in heterogeneous cross-flow catalysis system, acid and hydrogen peroxide is added in groove, make the waste water in pH regulator groove in acid, and ceaselessly stir, make it to mix; Waste water in pH regulator groove enters cross-flow catalytic reaction zone, and the completely rear waste water outflow of question response adjusts back groove to pH, adjusts back groove simultaneously add alkali (as NaOH) and flocculation agent (as polyacrylamide polyacrylamide PAM) at pH.The waste water that pH adjusts back in groove flow in settling tank certainly, and waste water can remove the suspended substance in a large amount of SS(water quality after precipitation).

More medium filter utilizes one or more filtration mediums, normal-temperature operation, acid and alkali-resistance, oxidation, and the pH scope of application is 2-13.The protector that system configuration is perfect and monitoring instrument, and there is backwashing function, the pollutents such as dirt are flushed away very soon, and water loss is few, can arrange full-automatic function by user's requirement.Under pressure, make stoste by the tactile flocculation of this medium, adsorb, retain, remove impurity, thus reach the object of filtration.Its in-built filler is generally: quartz sand, hard coal, particle porous pottery, manganese sand etc., user can according to practical situation choice for use.Its filtering accuracy, between 0.005-0.01m, can effectively remove colloidal particle and macromolecule organic.

Be mainly used in removing the suspended substance in water.This equipment coordinates with other water treating equipment, is widely used in all kinds of engineering of water treatment such as water supply purification, recirculating water purification sewage disposal.

Ultrafiltration (UF) (the present invention adopts ultrafiltration cartridge filter and ultra-filtration equipment) is a kind of membrane process between micro-filtration (MF) and nanofiltration (NF).Membrane pore size is between 0.1-5 μm.UF utilizes film " screening " to act on the membrane process carrying out being separated.Under the effect of static pressure difference, the particle being less than fenestra is by film, and the particle being greater than fenestra is then stopped on the surface of the film, make the particle varied in size be situated between to be separated, its filtering accuracy comparatively MF is higher, and thus fenestra is less, actual working pressure is also slightly high than MF, is generally 0.1-0.5MPa.

Reverse osmosis unit (the present invention adopts RO reverse osmosis cartridge filter, one-level RO reverse osmosis filter, secondary RO reverse osmosis filter) is the core of system pro desalting, and the water through reverse-osmosis treated can remove most inorganic salts and most organism, microorganism and colloid.Reverse osmosis desalination principle: reverse osmosis (RO) is the function by means of selecting through (semi-permeable) property film, take pressure difference as the membrane separation technique of impellent, when pressure added in system is greater than solution osmotic pressure, water molecules, constantly through film, flowing into pipe core through producing water flow passage, then flowing out in water side, impurity in water inlet, as: ion, organism, bacterium, virus etc. are trapped within the influent side of film, then flow out at dense water end (W.E.), thus reach the object of separation, desalination.Reverse osmosis membrane optimum operation temperature is 15-35 degree, if water inlet water temperature is too low, can not meet the demands, follow-up needs carries out water temperature-boosting measure.Reverse osmosis desalination part is made up of high-pressure pump, reverse osmosis unit, reverse osmosis washing unit etc.The suggestion of reverse osmosis unit membrane element selects that to bear pressure high, the good membrane module of mechanical tension, chemical erosion and pollution resistance.Reverse osmosis unit is made up of high-pressure pump, frame, reverse osmosis membrane and film pipe, back washing device etc., and is furnished with relevant under meter, conductivitimeter, tensimeter, sampling unit and relevant controlling elements.

Three-dimensional electrolysis oxidation reactor adds outside and produces electron motion in the positive pole of system, negative pole and multidimensional pole under the effect of mains power and there is following electron reaction equation:

O 2+4e+4H +---->2H2O4Cl--4e---->2Cl 2

Remove the salinity in the dense water of RO system dense water end (W.E.) outflow.It is carbonic acid gas and water that the hydrogen peroxide adding 500PPM in multidimension electrode produces electro-Fenton reaction in systems in which by the organic substance decomposing of RO fester.

Coking wastewater processing system provided by the invention can control and Non-follow control automatically.Before system cloud gray model, first open housing general supply.Coking chemical waste water in two-stage precipitation outlet sump is promoted in the reactive tank of preliminary sedimentation tank through intake pump.Water inlet the automatic control of pump, when in groove, liquid level is in low liquid level, intake pump starts automatically; When in groove, liquid level is in high liquid level, intake pump stops automatically.In reactive tank, add flocculation agent, after coagulating sedimentation, remove most suspended substance, waste water enters next unit: the heterogeneous cross-flow catalysis system of one-level.Open dosing pump, add a certain amount of acid and hydrogen peroxide toward one-level heterogeneous cross-flow catalysis.The water outlet of one-level heterogeneous cross-flow catalysis is from flowing into the heterogeneous cross-flow catalysis system of secondary.Secondary heterogeneous cross-flow catalysis system Ele-V(II) water outlet of system is from flowing to AOP-M system.AOP-M system Fen Sange district: pH regulation area, cross-flow catalytic domain and pH adjust back district.PH regulation area utilizes online pH meter to control its pH value at acid state.In pH regulation area, add hydrogen peroxide continuously by volume pump.The waste water of cross-flow catalytic domain pH regulation area through overflow port to cross-flow catalytic domain.Start reflux pump (before startup reflux pump, make the import of this pump, outlet valve is all in open mode) simultaneously, waste water is fully reacted in cross-flow catalytic domain.State that reflux pump should be in " often opening ".Until waste water after thoroughly reacting in cross-flow catalytic domain, overflow adjusts back district to pH.Online pH meter is utilized its pH value to be controlled between 8-8.5.When pH value is less than 8, the volume pump adding alkali starts automatically; When pH value is greater than 8.5, the volume pump adding alkali stops automatically.Adjust back district at pH, add PAM continuously by volume pump.

Waste water after the process of cross-flow catalysis system is from flowing in the settling tank of coagulative precipitation device.Supernatant liquor in settling tank is from flowing to UF inlet chest.Mud bottom settling tank promotes designated area through sludge pump.Open sludge pump (before startup sludge pump, confirm the import of this pump, outlet valve is all in open mode).The initiation culture of sludge pump is as follows: started once every four hours, run and automatically stop after ten minutes, circulate successively.Open the import of UF intake pump, outlet valve; Multiway valve on more medium filter is adjusted to running status, starts UF intake pump.The water of inlet chest is promoted to more medium filter through UF intake pump.Through UF intake pump, (when in UF inlet chest, liquid level is in high liquid level, UF intake pump starts automatically; When in UF inlet chest, liquid level is in low liquid level, UF intake pump stops automatically).More medium filter is for automatically to carry out cleaning, running: open enterprising valve and produce water valve, other valves are in closing condition.Recoil: open back-washing valve, upper valve, other valve closess, flush time is 15 minutes.Square impact: open enterprising valve, lower valve, other valve closess, flush time is 10 minutes.

RO system operation mode is as follows: when the difference increase by 15% poorer than first operating pressure of R/O operating pressure at different levels or water production rate decline 10%, then tackle film and carry out chemical cleaning operation.The performance of RO film affects by perhaps multifactorial, such as: working pressure, temperature, water inlet saltiness, product Water Sproading rate, system pH value.In normal operating process, the diaphragm in ro components can be subject to inorganic salt crust, microorganism, colloidal solid and insoluble organic pollution.In operating process, these pollutant sediments are on film surface, cause the decline of standardized product discharge and system ratio of desalinization or worsen simultaneously.When following situations occurs, need to clean membrane element: stdn water production rate reduces by more than 10%; Stdn desalination rate increases by more than 5%; Stdn pressure reduction between water inlet and dense water rises 15%; Above benchmark comparison condition takes from system through initial 48 hours postrun processing property.Must measure and record the pressure reduction (Δ P) of each section of pressurized vessel during regular job, along with in element, water entry is blocked, and Δ P will increase.It should be noted that element water production rate also can decline if inflow temperature reduces, this is normal and caused by the pollution of non-film.Pre-treatment, pressure-controlling increase that the is not normal or rate of recovery will cause the increase of the decline of water production rate or saturating salt amount.When the system of observing goes wrong, now element may not need cleaning, but should first consider this kind of reason.

Safety notice of the present invention is as follows:

When preparing scavenging solution, should guarantee before circulation enters element, all chemical obtain well dissolving and mixing.

After cleaning, suggestion adopts not rinsing (>=20 DEG C) system containing the water of chlorine residue of high-quality, recommendation reverse osmosis product water, if when there is no an etching problem to pipeline, and the available tap water through dechlorination and pretreated feedwater.Before returning to normal working pressure and flow, must be noted that to rinse with a large amount of scavenging solution under low flow and pressure.In addition, then in cleaning process, scavenging solution also can enter and produces water side, therefore, produce water must discharge more than 10 minutes or until clean to produce after starting up water limpid till.

In scavenging solution cycle period, during pH2-10, temperature can not more than 50 DEG C, and during pH1-12, temperature can not more than 30 DEG C.

Be described in detail specific embodiments of the invention above, but it is just as example, the present invention is not restricted to specific embodiment described above.To those skilled in the art, any equivalent modifications that the present invention is carried out and substituting also all among category of the present invention.Therefore, equalization conversion done without departing from the spirit and scope of the invention and amendment, all should contain within the scope of the invention.

Claims (9)

1. a coking wastewater processing system, it is characterized in that, comprise the two-stage precipitation outlet sump be connected successively, preliminary sedimentation tank, cross-flow catalysis system, coagulative precipitation device, more medium filter, ultrafiltration cartridge filter, ultra-filtration equipment, is produced from pond in ultrafiltration, RO reverse osmosis cartridge filter, one-level RO reverse osmosis filter, secondary RO reverse osmosis filter, also comprise three-dimensional electrolysis oxidation reactor, described one-level RO reverse osmosis filter is connected with three-dimensional electrolysis oxidation reactor with the dense water end (W.E.) of secondary RO reverse osmosis filter, the outlet of described three-dimensional electrolysis oxidation reactor is connected with the import of cross-flow catalysis system.
2. coking wastewater processing system according to claim 1, it is characterized in that, also comprise dense water collecting groove, the outlet of described ultra-filtration equipment is also connected with the import of dense water collecting groove, the outlet of described dense water collecting groove is connected with three-dimensional electrolysis oxidation reactor, and the outlet of described three-dimensional electrolysis oxidation reactor is connected with the import of cross-flow catalysis system.
3. the coking wastewater processing system according to claim 2 or 1, is characterized in that, described one-level RO reverse osmosis filter is connected with three-dimensional electrolysis oxidation reactor by dense water collecting groove with the dense water end (W.E.) of secondary RO reverse osmosis filter.
4. coking wastewater processing system according to claim 1, is characterized in that, described cross-flow catalysis system comprises the heterogeneous cross-flow catalytic unit of 1 heterogeneous cross-flow catalytic unit or multiple series connection.
5. the coking wastewater processing system according to claim 1 or 4, is characterized in that, described cross-flow catalysis system comprises the heterogeneous cross-flow catalytic unit of 2 series connection, is followed successively by one-level heterogeneous cross-flow catalytic unit and the heterogeneous cross-flow catalytic unit of secondary.
6. coking wastewater processing system according to claim 1, is characterized in that, the water purification end of described one-level RO reverse osmosis filter and secondary RO reverse osmosis filter, and the water purification end of secondary RO reverse osmosis filter is connected with production reclaiming system.
7. adopt a method for the coking wastewater processing system Treatment of Wastewater in Coking in claim 1-6 described in any one, it is characterized in that, comprise the following steps:
Step 1, coking chemical waste water enters preliminary sedimentation tank by two-stage precipitation outlet sump, adds flocculation agent, through flocculation sediment, except the suspended substance defocused in waste water;
Step 2, the waste water after step 1 processes flows into cross-flow catalysis system, and add acid and oxygenant, degradable organic pollutant, then adjust ph is to 8-8.5, adds flocculation agent;
Step 3, the waste water after step 2 processes flows in coagulative precipitation device, flocculation sediment, and supernatant liquor, successively through more medium filter, removes colloidal particle, macromolecule organic;
Step 4, the supernatant liquor after step 3 processes, further through ultrafiltration cartridge filter and ultra-filtration equipment filtration treatment, flows into ultrafiltration and produces pond;
Step 5, the waste water after step 4 processes through one-level RO reverse osmosis filter, secondary RO reverse osmosis filter reverse-osmosis treated removing inorganic salt, organism, microorganism and colloid, is discharged after reaching emission standard successively.
8. method according to claim 7, it is characterized in that, also comprise step 6: in step 5, one-level RO reverse osmosis filter and the dense water end (W.E.) waste water of secondary RO reverse osmosis filter enter three-dimensional electrolysis oxidation reactor, further except after freshen and organism, flow into cross-flow catalysis system, then repeating step 2,3,4 and 5.
9. method according to claim 8, is characterized in that, described step 6 at least repeats once.
CN201310230195.4A 2013-06-10 2013-06-10 A kind of Zero-discharge coked wastewater treatment system CN104230032B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201310230195.4A CN104230032B (en) 2013-06-10 2013-06-10 A kind of Zero-discharge coked wastewater treatment system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201310230195.4A CN104230032B (en) 2013-06-10 2013-06-10 A kind of Zero-discharge coked wastewater treatment system

Publications (2)

Publication Number Publication Date
CN104230032A CN104230032A (en) 2014-12-24
CN104230032B true CN104230032B (en) 2016-04-20

Family

ID=52219053

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201310230195.4A CN104230032B (en) 2013-06-10 2013-06-10 A kind of Zero-discharge coked wastewater treatment system

Country Status (1)

Country Link
CN (1) CN104230032B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104710055A (en) * 2015-03-31 2015-06-17 无锡元坤科技有限公司 Organic wastewater treatment method adopting boron-doped diamond electrode
CN104926035B (en) * 2015-06-11 2017-06-27 武汉钢铁(集团)公司 Coking comprehensive wastewater advanced treatment recycling technique and device
CN105884079A (en) * 2016-05-18 2016-08-24 南京海益环保工程有限公司 Brackish water reverse osmosis treatment technique
CN108681296A (en) * 2018-04-12 2018-10-19 大唐韩城第二发电有限责任公司 The control system of inner cold water automatic alkali adding device and the adder-subtractor with the system

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102942270A (en) * 2012-11-29 2013-02-27 湖南湘牛环保实业有限公司 Technology for deeply treating and recycling biochemical effluent of coking wastewater
CN203173928U (en) * 2013-04-08 2013-09-04 王余标 Coking wastewater treatment device

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102942270A (en) * 2012-11-29 2013-02-27 湖南湘牛环保实业有限公司 Technology for deeply treating and recycling biochemical effluent of coking wastewater
CN203173928U (en) * 2013-04-08 2013-09-04 王余标 Coking wastewater treatment device

Also Published As

Publication number Publication date
CN104230032A (en) 2014-12-24

Similar Documents

Publication Publication Date Title
US8062527B2 (en) Method and apparatus for desalinating sea water
Mallevialle et al. Water treatment membrane processes
Bani-Melhem et al. Development of a novel submerged membrane electro-bioreactor (SMEBR): performance for fouling reduction
US9180411B2 (en) Apparatus and process for treatment of water
CN103539288B (en) Industrial wastewater recovery method and wastewater recovery system
CN102786183B (en) Method for processing garbage leachate
CN102139979B (en) Method for treating coking waste water by electro-Fenton-coagulation combination process
AU2011233096B2 (en) Method for cleaning separation membrane module, and method for fresh water generation
CN103288309B (en) Coal gasification wastewater zero-emission treatment method, and application thereof
CN102515442B (en) Treatment method for recycling complex waste water in coal chemical industry
CN101343132B (en) Treatment method for wastewater of polyvinyl chloride (PVC) anticentripetal mother solution
KR100687095B1 (en) Electrodialysis reversal and electrochemical wastewater treatment process of compound containing nitrogen
CN102372400B (en) Hazardous waste handling center waste water integrated treatment system and method
US6582605B2 (en) Method of treating industrial waste waters
CN101851046B (en) Device for deep treatment and complete recovery of coking wastewater and application method thereof
Singhania et al. Immersed membrane bioreactors: an overview with special emphasis on anaerobic bioprocesses
US20090107915A1 (en) Treatment process and system for wastewater, process waters, and produced waters applications
EP2050723A1 (en) Method and integral system for treating water for cooling towers and processess requiring removal of silica from the water
CN102260009B (en) Method for processing dye wastewater
CN104016547B (en) A kind of coking waste water deep treatment zero-emission process
CN102452760B (en) Treatment method for recycle of oil field produced water
CN103265133B (en) Recycling method of papermaking advanced treatment wastewater based on chemical decalcification
CN101781039B (en) Technology for deeply processing coking wastewater through combining catalytic oxidation method and membrane separation technique
CN1686870A (en) Technique for processing reclamation of industrial wastewater from printing electronic circuit board
WO2005003044A1 (en) Method and system for treating wastewater

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
CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20160420

Termination date: 20170610