CN105502655B - A kind of activated sludge treatment method of brine waste - Google Patents
A kind of activated sludge treatment method of brine waste Download PDFInfo
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Abstract
The invention discloses a kind of activated sludge treatment methods of brine waste, method includes the following steps: (1) under the conditions of anoxic treatment, contacts brine waste with the material containing activated sludge, carry out the anoxic treatment of brine waste；(2) resulting mixture carries out Aerobic Process for Treatment after contacting；(3) by the mixed material return step (1) after the Aerobic Process for Treatment of part as the part material containing activated sludge, wherein, the partial size of at least activated sludge of 60 weight % in the mixed material after being back to the part Aerobic Process for Treatment in step (1) is not more than 1mm.The advantages of above-mentioned technical proposal according to the present invention promotes the degradation of hardly degraded organic substance and nitrification efficiency in brine waste, and does not need to add medicament and strengthen the aeration in the pond O, has operating cost low, no coupling product.
Description
Technical field
The present invention relates to a kind of activated sludge treatment methods of brine waste.
Background technique
Existing more mature saliferous wastewater processing technology generally uses at single-stage or two-stage air bearing and the combination of activated sludge
Science and engineering skill.A/O (anoxic/aerobic) technique is stable using its, Operation and Maintenance is simple, can the effectively advantages such as denitrogenation always as containing
The preferred technique of salt biological wastewater treatment.
By taking oil plant brine waste as an example, petroleum substance content is up to 500mg/L or more, pre- through multiple-unit oil removing
After processing, the raw water into A/O technique still contains a certain amount of colloidal type dispersed oil and oil emulsion, so that it is small to will appear these
The situation that oil droplet is adsorbed on active pollution index, coated.This aspect causes sludge mass transfer to be obstructed, active lower, another party
Face can generate a large amount of oil-containing excess sludges.Due to the presence of oil plant brine waste Poisoning, persistent organic pollutants, it is bound to
Cause the organic toxicity of the limitation of excess sludge.It is big, organic for oil plant brine waste biological treatment residue biological sludge yield
Toxicity is high, it is difficult to the problem of resource utilization, often carry out dangerous waste processing or burning disposal at present.Both processing modes are all deposited
The problem of energy consumption wastes and brings significant risk to environment.
Therefore, by the Optimal improvements of A/O process, sludge Sources decreasing and toxicity source abatement are realized, is to solve oil refining
The primary selection of brine waste excess sludge problem.Currently, common sludge Sources decreasing method is by adding in systems
Uncoupler or ozone aoxidized, excess sludge is cracked using means such as supercritical ultrasonics technologies after flow back into aeration tank by micro- life
Object degradation, thus achieve the purpose that on source reduce excess sludge production, but these methods there are secondary pollution, be difficult to control,
The problems such as operating cost is high.
Remaining tiny oil droplets are adsorbed on active pollution index, are coated in oil plant brine waste, and then cause substrate
(organic substrates or ammonia nitrogen etc.) are difficult to sludge wadding body active region mass transfer, and the dissolved oxygen (DO) of aerobic tank (pond O) is to sludge wadding body
Internal mass transfer is obstructed, and causes sludge activity low, and the denitrifying carbon source in anaerobic pond (pond A) is insufficient, so that at brine waste
Managing effect reduces.For this problem, in existing engineer application, often by strengthening the air aeration intensity in the pond O to solve this
Problem.It is bound to cause the energy consumption waste of air aeration in this way.
Summary of the invention
The purpose of the invention is to overcome above-mentioned preceding defect, providing one kind can be improved activity of activated sludge, at anoxic
The carbon source of reason, and not will cause the activated sludge treatment method of secondary pollution, lower-cost brine waste.
To achieve the goals above, the present invention provides a kind of activated sludge treatment method of brine waste, this method packets
It includes following steps: (1) under the conditions of anoxic treatment, contacting brine waste with the material containing activated sludge, carry out brine waste
Anoxic treatment；(2) resulting mixture carries out Aerobic Process for Treatment after contacting；(3) by the mixed material after the Aerobic Process for Treatment of part
Return step (1) is as the part material containing activated sludge, wherein at least 60 weights in the material containing activated sludge
The partial size for measuring the activated sludge of % is not more than 1mm, preferably 0.5-1mm.
Preferably, during being back to step (1) by the mixed material after the part Aerobic Process for Treatment, to described
Mixed material after the Aerobic Process for Treatment of part carries out eddy flow processing, after making the part Aerobic Process for Treatment being back in step (1)
Mixed material in the partial size of at least activated sludge of 60 weight % be not more than 1mm, eddy flow processing in cyclone into
Row.It is highly preferred that the condition of eddy flow processing makes speed of the mixed material after the part Aerobic Process for Treatment in cyclone
It spends gradient and is not less than 1100S-1, preferably 2800-5600S-1。
Preferably, this method further includes that carbon dioxide is passed through during carrying out Aerobic Process for Treatment, and carbon dioxide is passed through
Amount is so that the volume ratio of the carbon dioxide and oxygen that are passed through is 0.25-1:1.
Above-mentioned technical proposal according to the present invention passes through the mixing after the part Aerobic Process for Treatment that will be back in step (1)
The size controlling of at least activated sludge of 60 weight % in material is being not more than 1mm, in the range of preferably 0.5-1mm, energy
Enough make the exposure release of the organic matters such as polysaccharide and the protein in sludge, with the organic carbon in mixed material supplement anoxic treatment
The denitrification denitrogenation efficiency during anoxic treatment is improved in source；And in the case where preferably handling by eddy flow, fluid is carried out
Shearing, releases the small oil droplet of Sludge Surface further, the activity of sludge is effectively improved, and sludge circle is enhanced
The mass-transfer performance in face promotes the efficiency of hardly degraded organic substance degradation and nitrification in brine waste.Therefore, the present invention does not need to throw
The advantages of adding medicine and the aeration for strengthening the pond O have operating cost low, no coupling product.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
In the following description of the present invention, the term " hydraulic detention time " used refers to brine waste to be processed in reactor
The average reaction time of microbial action in interior mean residence time, that is, brine waste and reactor, therefore, if instead
The dischargeable capacity for answering device is V (m3), water velocity is Q (m3/ h), then: when hydraulic detention time (HRT)=V/Q, i.e. hydraulic retention
Between be equal to the ratio between reactor dischargeable capacity and water velocity.
Anoxic treatment is the main stage that anti-nitration reaction occurs, and anti-nitration reaction refers under anaerobic condition, denitrification
Nitrite nitrogen, nitrate nitrogen in waste water is reduced into gaseous nitrogen (N by bacterium2) process.Denitrifying bacterium is heterotroph microorganism,
Belong to facultative bacteria, in anaerobic condition, using the oxygen in nitrate as electron acceptor, with the organic matter (BOD in sewage more
Ingredient) it is used as electron donor, energy is provided and is oxidized stabilization.
Aerobic Process for Treatment is the main stage that nitration reaction occurs, and nitration reaction refers under aerobic state, nitrococcus benefit
It is carbon source by NH with inorganic carbon4 +It is converted to nitrite (NO2 -), then nitrite-oxidizing is nitrate (NO by nitrifier3 -)
Process.
Denitrifying bacterium, nitrococcus and nitrifier are the micro- life being conventionally present in the activated sludge for purification of water quality
Object, details are not described herein.
" COD " i.e. COD is an index for indicating reducing substances are how many in water, and COD value is bigger, illustrates water
Body is more serious by the pollution of organic matter, and all COD values involved in the present invention are potassium dichromate oxidation (GB11914-
89) numerical value measured.
" ammonia-nitrogen content " refer in every liter of water in the form of free ammonia and ammonium ion existing for nitrogen amount, be abbreviated as NH4 +-N。
" total nitrogen level " is abbreviated as TN in terms of the nitrogenous milligram number of every liter of water.
When " velocity gradient " refers to that fluid flows between two interfaces, due to the presence of frictional force between material, make speed
Difference occurs for the flowing velocity of gradient internal fluid and fluid and velocity gradient interface contacts, generates the speed of a gradual change
Field, referred to as velocity gradient or cutting speed rate, shear rate.
On the one hand, the present invention provides a kind of activated sludge treatment methods of brine waste, method includes the following steps:
(1) it under the conditions of anoxic treatment, contacts brine waste with the material containing activated sludge, carries out the anoxic treatment of brine waste；
(2) resulting mixture carries out Aerobic Process for Treatment after contacting；(3) by the mixed material return step (1) after the Aerobic Process for Treatment of part
As the part material containing activated sludge, wherein the mixture after being back to the part Aerobic Process for Treatment in step (1)
The partial size of at least activated sludge of 60 weight % in material is not more than 1mm, preferably 0.5-1mm.
Hereinafter, " mixed material after the part Aerobic Process for Treatment being back in step (1) " is together simply referred to as " returning
Flow liquid ".
It was found by the inventors of the present invention that being crushed to the activated sludge in the phegma, and make wherein at least 60
The partial size of the activated sludge of weight % is not more than 1mm, preferably 0.5-1mm, and the exocytosis that can be released effectively in sludge is more
The organic matters such as sugar and protein, and recycled in the pond A as organic carbon source.In addition, the broken of sludge is accompanied by sludge institute
The removing of the oily phase of package, the activity after de-oiling is dissociated, and flora can formation be high living again in the biological treatment process in the pond A to the pond O
Property sludge can be effectively in sludge Sources decreasing with the biochemical activity of consolidation system, and promotion system biochemical activity, thus
Complete the present invention.
According to the present invention, in situations where it is preferred, the partial size of activated sludge whole in the material containing activated sludge
No more than 2mm.
Although by least the size controlling of the activated sludge of 60 weight % is being not more than 1mm in the phegma, preferably
The purpose of the present invention can be realized in 0.5-1mm.But it was found by the inventors of the present invention that being handled by eddy flow so that in the phegma
At least the partial size of the activated sludge of 60 weight % is not more than 1mm, preferably 0.5-1mm, that is, after the part Aerobic Process for Treatment
Mixed material be back to step (1) during, to after the part Aerobic Process for Treatment mixed material carry out eddy flow processing, come
The grain of at least activated sludge of 60 weight % in mixed material after making the part Aerobic Process for Treatment being back in step (1)
Diameter is not more than 1mm, and the performance of sludge can be made to be further enhanced.The eddy flow processing carries out preferably in cyclone, is
The condition of realization above-mentioned requirements, the eddy flow processing makes velocity gradient of the mixed material in cyclone preferably not low
In 1100S-1, more preferably 2800-5600S-1。
Although within the scope of the invention can be effectively by the velocity gradient control of the mixed material in cyclone
Realize goal of the invention of the invention.But it was found by the inventors of the present invention that carry out following control by the condition for handling eddy flow,
The exocytosis in sludge in processed mixed material can more effectively discharge, and be more conducive to activated sludge release
Thallus out forms the sludge wadding body of high activity again.The condition of eddy flow processing preferably includes: with the cyclone into
On the basis of material mouth diameter is 0.02-0.04m, the feed flow rate of cyclone is 1-8m/s, and feed inlet pressure is not less than 0.03MPa；
The feed inlet pressure of the cyclone is greater than discharge port pressure, pressure difference 0.03-0.15MPa.The present invention it should be pointed out that
The intake port of the cyclone increases, and the charging rate of the phegma will reduce, pressure will reduce.
According to the present invention, the phegma in cyclone in the process of processing, further include to the phegma into
Row overflow, the flow of the overflow are the 2-5 volume % of the phegma feed rate.By controlling the flow of the overflow,
It can effectively guarantee velocity gradient of the phegma in cyclone, so that at least 60 weight % in the phegma
Activated sludge partial size be not more than 1mm, preferably 0.5-1mm.
According to the present invention, the method also includes removing the tiny oil droplets to fall off after eddy flow processing, to realize point of grease
From to reduce the oil content of water outlet.According to the method for the present invention, the tiny oil droplets to fall off can in cyclone Strong shear stress
It is separated from the water under effect, so as to be discharged from the overflow port of cyclone.Herein it should be noted that working as the phegma oil-containing
When more, need to be collected separately the overflowing liquid being discharged from overflow port, returned again to after oil removing into step (1)；When the phegma
When oil-containing is less, the overflowing liquid being discharged from overflow port can be returned directly in step (1).
Present inventor has further discovered that by being passed through carbon dioxide during Aerobic Process for Treatment, and control dioxy
The intake for changing carbon makes the volume ratio for the carbon dioxide and oxygen being passed through for 0.25-1:1, preferably 0.5-1:1, can be further
Reduce the ammonia nitrogen of treated brine waste, the content of nitrate and total nitrogen.Wherein, the body of the oxygen and carbon dioxide
Carbon dioxide in product ratio only refers to the amount for the carbon dioxide being additionally passed through.Wherein, oxygen and being passed through for carbon dioxide can use
Method well known in the art carries out, and details are not described herein by the present invention.
Although method of the invention can be suitable for various brine wastes, it was found by the inventors of the present invention that of the invention
Method is especially suitable for handling the brine waste that oil plant discharges.
The COD value of the brine waste is 500-800mg/L, NH4 +- N is 50-100mg/L, NO3 -- N is 0-10mg/L,
Preferably 8-12mg/L, the content of total nitrogen are 50-150mg/L, and the content of petroleum substance is 800-1500mg/L, the content of SS
For 300-600mg/L, the content of sulfide is 15-25mg/L, and basicity (with calcium carbonate) is 200-300mg/L, and pH value is
7.5-9.5。
Wherein, term " petroleum substance " refers to the hydrocarbons such as alkane, aromatic hydrocarbons, asphalitine, colloid.
According to the present invention, in hypoxic/anaerobic technique, when the flow and step of the phegma in return step (1)
It (1), can be significant by flowing back broken sludge wadding body when the ratio for carrying out the flow of the former brine waste of anoxic treatment in is 2-4
Decrement discharge sludge.It is carried out in the flow of the mixed material after the part Aerobic Process for Treatment in return step (1) and step (1)
The ratio of the flow of the former brine waste of anoxic treatment is referred to as " internal reflux ratio " or " return current ratio of the mixed liquid ".It is wherein, described that " original contains
Salt waste water " is the brine waste for initially carrying out anoxic treatment.
In the present invention, the condition of anoxic treatment and Aerobic Process for Treatment can be the condition that this field routinely uses, the anoxic
The condition of processing preferably includes: dissolved oxygen is no more than 1mg/L (such as 0.5-1mg/L), and temperature is 10-40 DEG C, hydraulic detention time
For 2-6h.The condition of the Aerobic Process for Treatment preferably includes: dissolved oxygen 2-4mg/L, and temperature is 10-40 DEG C, hydraulic detention time
For 8-16h.
In the present invention, anoxic treatment and Aerobic Process for Treatment series connection are carried out, and are not required particularly its specific series system,
For example, can be the series system of anaerobic-aerobic.As needed, can also be arranged before anoxic treatment and Aerobic Process for Treatment tight
The Anaerobic Treatment (dissolved oxygen 0) of lattice control dissolved oxygen.It is 10-40 DEG C that the condition of Anaerobic Treatment, which generally includes temperature, and waterpower is stopped
Staying the time is 2-6h.
In the present invention, activated sludge commonly used in the art can be used and carry out biological denitrificaion, under preferable case, anoxic
The sludge loading for the activated sludge that processing and/or Aerobic Process for Treatment use is 0.15-0.5kgCOD/ (kg sludge d).
In order to make full use of the activated sludge, the invention also includes by the mixed material after remaining part Aerobic Process for Treatment
Be separated by solid-liquid separation, and obtained activated sludge return step (1) will be separated by solid-liquid separation to add in entire processing system so that
Sludge concentration balance.Specifically operate it is known to those skilled in the art, the present invention details are not described herein.
In order to further increase effluent characteristics, method of the invention can also be included in into Aerobic Process for Treatment and anoxic treatment
Before, brine waste is first subjected to homogeneous and dissolved air flotation.The homogeneous usually passes through stirring and realizes, the condition of dissolved air flotation is logical
It often include: relative to 1000m3Brine waste to be processed, the flow for the gas being passed through is preferably 200-400m3/ h, temperature are
0-40 DEG C, time 0.5-1.0h.
The present invention will be described in detail by way of examples below.In following embodiment,
The measuring method of COD value is dichromate titration (GB11914-89)；
The measuring method of ammonia-nitrogen content (NH4+-N) is Berthelot spectrophotometry (HJ 535-2009)；
The measuring method of total nitrogen level (NO3--N) is that alkaline chitinase clears up ultraviolet spectrophotometry (HJ 636-
2012)；
The measuring method of petroleum content is infrared spectrophotometer (HJ 637-2012), and the measuring method of SS content is
Gravimetric method (GB 11901-89)；
The measuring method of sulfide content is directly to develop the color spectrophotometry (GB/T 17133-1997)；
The measuring method of basicity is titration (GB/T 15451-95)；
The velocity gradient of phegma is measured by U.S. YSI FlowTracker doppler velocimeter in cyclone；
The partial size of activated sludge by Malvem laser particle instrument measurement (Malvem Mastersizer 2000,
Malvem, UK) measurement；
The inlet diameter of cyclone is 0.02m.
The water quality of brine waste used in embodiment is as shown in table 1.
Table 1
Embodiment 1
Active sludge treatment (including anoxic treatment and Aerobic Process for Treatment) is carried out to brine waste 1, the method for the processing is pressed
According to " the 342-344 pages of " Water Pollution Control Engineering ": Water Pollution Control Engineering, Wang Yu chief editor, Lin Fengkai associate editor, chemical industry
Publishing house, 2008 " carry out.Unlike, cyclone is set on the aerobic reflux pipeline for returning to anaerobism, cyclone feed inlet
Flow velocity is 4-6m/s, and feed pressure 0.10-0.15MPa, the pressure difference of inlet port and outlet port is 0.10-0.15MPa, eddy flow
The flow of the overflow port of device is 3.5 volume % of inlet flow rate, and the mixed material (phegma) from Aerobic Process for Treatment is in cyclone
The velocity gradient of middle eddy flow is 4000S-1.The partial size of the active pollution index of 80 weight % is 0.5-1mm after eddy flow, and institute is active
The partial size of sludge wadding body is no more than 2mm.Processing result is as shown in table 2.
Embodiment 2
Active sludge treatment (including anoxic treatment and Aerobic Process for Treatment) is carried out to brine waste 2.The method of the processing is pressed
According to " the 342-344 pages of " Water Pollution Control Engineering ": Water Pollution Control Engineering, Wang Yu chief editor, Lin Fengkai associate editor, chemical industry
Publishing house, 2008 " carry out.Unlike, cyclone is set on the aerobic reflux pipeline for returning to anaerobism, cyclone feed inlet
Flow velocity is 1-4m/s, and feed pressure 0.03-0.06MPa, the pressure difference of inlet port and outlet port is 0.06MPa, cyclone
The flow of overflow port is 2 volume % of inlet flow rate, mixed material (phegma) eddy flow in cyclone from Aerobic Process for Treatment
Velocity gradient be 2800S-1.The partial size of the active pollution index of 60 weight % is 0.5-1mm after eddy flow, all activated sludge waddings
The partial size of body is no more than 2mm.Processing result is as shown in table 2.
Embodiment 3
Active sludge treatment (including anoxic treatment and Aerobic Process for Treatment) is carried out to brine waste 3.The method of the processing is pressed
According to " the 342-344 pages of " Water Pollution Control Engineering ": Water Pollution Control Engineering, Wang Yu chief editor, Lin Fengkai associate editor, chemical industry
Publishing house, 2008 " carry out.Unlike, cyclone is set on the aerobic reflux pipeline for returning to anaerobism, cyclone feed inlet
Flow velocity is 6-8m/s, and feed pressure 0.08-0.10MPa, the pressure difference of inlet port and outlet port is 0.10MPa, cyclone
The flow of overflow port is 5 volume % of inlet flow rate, the speed ladder of the eddy flow in cyclone of the mixed material from Aerobic Process for Treatment
Degree is 5600S-1.The partial size of the active pollution index of 90 weight % is 0.5-1mm, the partial size of all active pollution index after eddy flow
No more than 2mm.Processing result is as shown in table 2.
Embodiment 4-6
Brine waste 1 is handled according to the method for embodiment 1, unlike, during Aerobic Process for Treatment, become better
It is passed through carbon dioxide in oxygen unit, the amount for the carbon dioxide being passed through makes the volume of carbon dioxide and oxygen be respectively 0.8:1,
0.5:1 and 1:1.
Comparative example 1
Biological denitrificaion is carried out according to the method for embodiment 1, unlike, it is not set on the aerobic reflux pipeline for returning to anaerobism
Cyclone is set, but is directly back to anaerobic stages.
Table 2
As can be seen from Table 2, using technical solution of the present invention, by the way that the activity of at least 60 weight % in phegma is dirty
For the size controlling of mud in the case where the partial size of all active pollution index of 0.5-1mm is no more than 2mm, the emission reduction of sludge can
Reach 60 volume %, and brine waste has also obtained effectively handling.In the feelings for being preferably passed through carbon dioxide to Aerobic Process for Treatment
Under condition, the content of the ammonia nitrogen of the brine waste that can further decrease that treated, nitrate and total nitrogen.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (11)
1. a kind of activated sludge treatment method of brine waste, method includes the following steps:
(1) under the conditions of anoxic treatment, contact brine waste with the material containing activated sludge, at the anoxic for carrying out brine waste
Reason；
(2) resulting mixture carries out Aerobic Process for Treatment after contacting；
(3) by the mixed material return step (1) after the Aerobic Process for Treatment of part as the part material containing activated sludge；
Wherein, at least activity of 60 weight % in the mixed material after being back to the part Aerobic Process for Treatment in step (1)
The partial size of sludge is not more than 1mm；
Wherein, good to the part during being back to step (1) by the mixed material after the part Aerobic Process for Treatment
Oxygen treated mixed material carries out eddy flow processing, to make the mixing after the part Aerobic Process for Treatment being back in step (1)
The partial size of at least activated sludge of 60 weight % in material is not more than 1mm, and the eddy flow processing carries out in cyclone；
Wherein, this method further includes that carbon dioxide is passed through during carrying out Aerobic Process for Treatment, and the intake of carbon dioxide makes
The volume ratio of the carbon dioxide and oxygen that are passed through is 0.25-1:1.
2. according to the method described in claim 1, wherein, the partial size of activated sludge is not more than in the material containing activated sludge
2mm。
3. according to the method described in claim 1, wherein, after the condition of the eddy flow processing makes the part Aerobic Process for Treatment
Velocity gradient of the mixed material in cyclone is not less than 1100S-1。
4. according to the method described in claim 1, wherein, after the condition of the eddy flow processing makes the part Aerobic Process for Treatment
Velocity gradient of the mixed material in cyclone is 2800-5600S-1。
5. according to claim 1, method described in 3 or 4, wherein the condition of the eddy flow processing includes: with the cyclone
On the basis of intake port is 0.02-0.04m, the feed flow rate of cyclone is 1-8m/s, and feed inlet pressure is not less than
0.03MPa；The feed inlet pressure of the cyclone is greater than discharge port pressure, pressure difference 0.03-0.15MPa.
6. according to the method described in claim 5, wherein, the condition of the eddy flow processing includes: with the charging of the cyclone
On the basis of mouth diameter is 0.02-0.04m, the feed inlet pressure of cyclone is 0.03-0.15MPa.
7. according to the method described in claim 1, wherein, this method further include: the mixture after the part Aerobic Process for Treatment
Material in the process of processing, carries out overflow, the overflow to the mixed material after the part Aerobic Process for Treatment in cyclone
Flow be the part Aerobic Process for Treatment after mixed material feed rate 2-5 volume %.
8. according to the method described in claim 1, wherein, this method further includes, by the mixture after remainder Aerobic Process for Treatment
Material is separated by solid-liquid separation, and will be separated by solid-liquid separation obtained activated sludge return step (1) as dirty containing activity described in another part
The material of mud.
9. according to the method described in claim 1, wherein, the COD value of the brine waste is 500-800mg/L, NH4 +- N is
50-100mg/L, NO3 -- N is 0-10mg/L, and the content of total nitrogen is 50-150mg/L, and the content of petroleum substance is 800-
1500mg/L, the content of suspended matter are 300-600mg/L, and the content of sulfide is 15-25mg/L, is with the basicity of calcium carbonate
200-300mg/L。
10. according to the method described in claim 1, wherein, the brine waste is the brine waste from oil plant.
11. according to the method described in claim 1, wherein, the mixing after being back to the part Aerobic Process for Treatment in step (1)
The ratio that the flow of the brine waste of anoxic treatment is carried out in the flow and step (1) of material is 2-4.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101357815A (en) * | 2008-08-14 | 2009-02-04 | 北京环利科环境工程技术有限公司 | EH-BFB biochemical denitrification dephosphorization technique |
| CN103739156A (en) * | 2013-12-18 | 2014-04-23 | 杭州智水水务科技有限公司 | Method for performing biological denitrification of wastewater by using residual sludge and biological denitrification system for implementing same |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101357815A (en) * | 2008-08-14 | 2009-02-04 | 北京环利科环境工程技术有限公司 | EH-BFB biochemical denitrification dephosphorization technique |
| CN103739156A (en) * | 2013-12-18 | 2014-04-23 | 杭州智水水务科技有限公司 | Method for performing biological denitrification of wastewater by using residual sludge and biological denitrification system for implementing same |
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