CN104909524A - Method for processing oil cracking catalyst industrial wastewater through electric flocculation-canon (CANON) combination - Google Patents
Method for processing oil cracking catalyst industrial wastewater through electric flocculation-canon (CANON) combination Download PDFInfo
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- CN104909524A CN104909524A CN201510400190.0A CN201510400190A CN104909524A CN 104909524 A CN104909524 A CN 104909524A CN 201510400190 A CN201510400190 A CN 201510400190A CN 104909524 A CN104909524 A CN 104909524A
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- flocculation
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- factory effluent
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Abstract
The invention discloses a method for processing oil cracking catalyst industrial wastewater through electric flocculation-canon (CANON) combination, which relates to a method for processing catalyst production wastewater, and solves the problems that oil cracking catalyst industrial wastewater pre-treatment technology is large in coagulation reagent dosage at present, is easy to cause secondary pollution, large in floor space of equipment and capital investment, high in aeration consumption of biochemical treatment process, large in dosage of denitrifying denitrification carbon sources and low in nitrogen removal efficiency and the like. The method for processing the catalyst production wastewater comprises the steps: 1 electric flocculation pretreatment; and 2 CANON process. The method for processing oil cracking catalyst industrial wastewater through electric flocculation-CANON combination just adopts the two steps of the electric flocculation pretreatment and the CANON process to process the oil cracking catalyst industrial wastewater, has the advantages of simple method, short technological process, small floor space and low investment and operation cost and the like, and is excellent and steady in water quality.
Description
Technical field
The present invention relates to a kind for the treatment of process of catalyst production waste water.
Background technology
It is with kaolin, aluminum oxide, molecular sieve and ammonium sulfate, ammonium chloride etc. for raw material that catalyst of cracking petroleum is produced, and makes through 5 large operations such as plastic, spraying dry, high-temperature roasting, exchange filtration, air stream dryings.Therefore, the waste water produced in catalyst production process has following characteristics due to its raw material adopted and production technique: 1) NH
4 +-N concentration is high; 2) SS and turbidity high; 3) organic concentration is lower, and waste water C/N is low; 4) containing phenol, heavy metal etc., microorganism is produced to the material of poisoning.
The research being directed to process catalyst of cracking petroleum factory effluent both at home and abroad mainly concentrates on the process of the materials such as suspended substance (SS), high ammonia nitrogen.The pretreatment technology that catalyst of cracking petroleum production wastewater treatment is commonly used at present is coagulating sedimentation, and it is large that the method exists coagulated agent dosage, easily causes secondary pollution problem, and treatment facility floor space and initial cost large.NH in catalyst of cracking petroleum factory effluent
4 +-N treatment process adopts traditional biological denitrification process, there is aeration energy consumption high, and denitrification denitrogenation carbon source dosage is large, the problems such as nitric efficiency is low.Variation water quality simultaneously due to cracking catalysis agent production waste water is large, and coagulating sedimentation pre-treatment effluent quality is unstable, and the problem of regulate and control operation complexity is particularly outstanding; Cause the denitrification effect of later stage water treatment to be also difficult to control and stablize, effluent quality cannot ensure.
Summary of the invention
The object of the invention is to solve current catalyst of cracking petroleum factory effluent pretreatment technology coagulated agent dosage large, easily causing secondary pollution, greatly, pre-treatment effluent quality is unstable for treatment facility floor space and initial cost; Traditional biological denitrification process aeration energy consumption is high, and carbon source dosage is large, and nitric efficiency is low, and variation water quality is comparatively large, and effluent quality such as cannot to ensure at the problem, and the method for a kind of electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent provided.
The method of electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent is carried out according to the following steps:
One, cracking catalysis agent production waste water pH value is adjusted to 8.0 ~ 9.0, then carries out electricity flocculation;
Two, CANON technique, namely can be out of the water, and completes catalyst of cracking petroleum production wastewater treatment.
The advantages such as the inventive method only adopts electricity flocculation and CANON technique 2 steps namely to complete process to catalyst of cracking petroleum factory effluent, has that method is simple, technical process is short, and floor space is little, invest and working cost is low, effluent quality is excellent and stable.
Adopt electricity flocculation in the inventive method, add without chemical agent, avoid secondary pollution; Water outlet total dissolved solid (TDS) content is low; And in the face of the catalyst of cracking petroleum factory effluent that variation water quality is larger, electricity flocculation shows good flocculating effect and impact resistance, can remove the COD of about 30% while reducing former water high concentrtion.
Adopt AOB and the ANAMMOX bacterium in CANON technique to be all autotrophic bacteria in the inventive method, therefore can save the aeration rate of 63% and the additional carbon of nearly 100%; In addition the time in epoch (being about 15d) that ANAMMOX bacterium is longer, so the excess sludge production of CANON reactor is little, there is the advantage that running cost is low, application prospect is large.
Because variation water quality is large, NH
4 +-N concentration is high, SS and turbidity high, organic concentration is lower, waste water C/N is low, and containing phenol, heavy metal, after catalyst of cracking petroleum production wastewater treatment, water quality is difficult to up to standard.And adopt the guarantee effluent quality that the inventive method not only can be stable, and pollutants removal rate is high, water quality is good.The water body general technology step that, water quality larger for variation water quality is complicated is many, control difficulty is large, running cost is high, initial cost is large, floor space is large; But, the present invention electricity consumption flocculation and CANON2 step, and each step is convenient to control, and has the advantage that running cost is low, initial cost is little, floor space is little.
Embodiment
Technical solution of the present invention is not limited to following cited embodiment, also comprises the arbitrary combination between each embodiment.
Embodiment one: the method for present embodiment electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent is carried out according to the following steps:
One, cracking catalysis agent production waste water pH value is adjusted to 8.0 ~ 9.0, then carries out electricity flocculation;
Two, CANON technique, namely can be out of the water, and completes catalyst of cracking petroleum production wastewater treatment.
The method effluent quality of present embodiment electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent remains at turbidity <30NTU, NH
4 +-N concentration <10mgL
-1, NO
2 --N concentration <5mgL
-1, COD concentration <100mgL
-1, NO
3 --N concentration <40mgL
-1.
In present embodiment method, electricity flocculation ensures the water quality of CANON technique water inlet, slows down heavy metal and organism to the impact of anaerobic ammonia oxidizing bacteria.
There is part heterotrophic bacteria in CANON reactor, part COD can be utilized to carry out growth metabolism.Due to CANON inside reactor mass transfer, in reactor, there is a small amount of denitrifying bacterium, utilize organic carbon source to reach the effect removing COD by anti-nitration reaction.
The granule sludge of CANON technique inoculation has good settling condition, makes organism be retained in reactor; Do not need back flushing power consumption, have biomembranous function concurrently again.Meanwhile, CANON technique can greatly reduce NO and N
2o isothermal chamber gas purging, utilizes CANON technique in one-part form reactor, realize the good cometabolism denitrogenation of AOB and ANAMMOX, and compared with two-part SHARON+ANAMMOX technique, technique is convenient to control, floor space is little, application prospect is larger.
Embodiment two: the difference of present embodiment and embodiment one is: output voltage≤30V, outward current≤5A during step one electricity flocculates.Other step and parameter identical with embodiment one.
Embodiment three: the difference of present embodiment and embodiment one or two is: step one electricity flocculates and adopts current density to be 25mAcm
-2direct current, polar plate spacing be 1.5cm.Other step and parameter identical with embodiment one or two.
Embodiment four: the difference of one of present embodiment and embodiment one to three is: the electric flocculation time of step one is 20 ~ 60min.Other step and parameter identical with one of embodiment one to three.
Embodiment five: the difference of one of present embodiment and embodiment one to three is: the electric flocculation time of step one is 25min.Other step and parameter identical with one of embodiment one to three.
Embodiment six: the difference of one of present embodiment and embodiment one to five is: step one electricity flocculation electrode connecting mode is acyclic type, carries out once pole every 5 cycles.Other step and parameter identical with one of embodiment one to five.
Present embodiment every 5 cycles carry out once pole in case electrode passivation.
Embodiment seven: the difference of one of present embodiment and embodiment one to six is: in the flocculation of step one electricity, electrode pad is aluminium sheet.Other step and parameter identical with one of embodiment one to six.
Present embodiment electrode pad upper end is connected with direct supply by copper cash; In order to prevent copper cash from dissolving the open circuit causing pole plate and power supply in electrolytic process, the upper end of pole plate will keep certain safe distance apart from effective liquid level of electric flocculation reaction groove.
Embodiment eight: the difference of one of present embodiment and embodiment one to seven is: carry out aeration while of the flocculation of step one electricity.Other step and parameter identical with one of embodiment one to seven.
Carry out aeration while the flocculation of present embodiment electricity, aeration has stirring action, can ensure that the metallic cation that positive plate is separated out can both contact with waste water fully with the bubble that negative electrode produces.
And the dissolved oxygen that aeration provides also participates in electricity flocculation to oxidizing reaction organic in catalyst of cracking petroleum factory effluent, improves pollutant removal further, and shortens electric flocculation time.
Embodiment nine: the difference of one of present embodiment and embodiment one to eight is: the useful volume of the electric flocculation reaction groove of step one electricity flocculation is 10L.Other step and parameter identical with one of embodiment one to eight.
Embodiment ten: the difference of one of present embodiment and embodiment one to nine is: controlling dissolved oxygen in step 2 CANON technique is 0.5 ± 0.05mg/L, temperature of reaction is 30 ± 0.5 DEG C, pH value is 7.5 ~ 8.2, and hydraulic detention time is 15 ~ 20h.Other step and parameter identical with one of embodiment one to nine.
Embodiment 11: the difference of one of present embodiment and embodiment one to ten is: the expanded granular sludge bed EGSB of step 2 CANON technology utilization, the effective volume of reactor is 1.4L, and aspect ratio is 20.Other step and parameter identical with one of embodiment one to ten.
Embodiment 12: the difference of one of present embodiment and embodiment one to ten one is: step 2 CANON process reactor takes shading treatment.Other step and parameter identical with one of embodiment one to ten one.
Present embodiment takes shading treatment to CANON process reactor, can prevent illumination from hindering the growth of anaerobic ammonia oxidizing bacteria.
Embodiment 13: the difference of one of present embodiment and embodiment one to ten two is: the postprecipitation 30min of step one electricity flocculation.Other step and parameter identical with one of embodiment one to ten two.
Embodiment 14: the difference of one of present embodiment and embodiment one to ten three is: the step 2 CANON technique starting period inoculates CANON granule sludge, sludge concentration is 1.5gL
-1.Other step and parameter identical with one of embodiment one to ten three.
Embodiment 1
The method of electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent is carried out according to the following steps:
One, by cracking catalysis agent production waste water through natural subsidence 10min, pH value is adjusted to 8.0 ~ 9.0 afterwards, then carry out electricity flocculation, precipitation 30min;
Two, electricity flocculation water outlet enters CANON technique and carries out denitrogenation after water quality regulation, namely can be out of the water, completes catalyst of cracking petroleum production wastewater treatment;
Wherein, in the flocculation of step one electricity, output voltage is 5V, and outward current is 1.35A; The flocculation of step one electricity adopts current density to be 25mAcm
-2direct current, polar plate spacing be 1.5cm, electric flocculation time is 25min, and electrode connecting mode is acyclic type;
Carry out aeration while the flocculation of step one electricity, aeration rate reaches 15L/min;
Controlling dissolved oxygen in step 2 CANON technique is 0.5 ± 0.05mg/L, and temperature of reaction is 30 ± 0.5 DEG C, and pH value is 7.5 ~ 8.2, and hydraulic detention time is 15 ~ 20h; Step 2 CANON technology utilization EGSB reactor is carrier, and reactor effective volume is 1.4L, and aspect ratio is 20; CANON process reactor takes shading treatment; Step 2 CANON technique starting period inoculation CANON granule sludge, sludge concentration is 1.5gL
-1.。
Utilize the present embodiment process catalyst of cracking petroleum factory effluent, and monitor catalyst of cracking petroleum factory effluent raw water quality and effluent quality detected result is as shown in table 1.
Table 1
In 15d, Process for Effluent water quality reaches turbidity <30NTU, NH
4 +-N<10mgL
-1, NO
2 --N<5mgL
-1, COD<100mgL
-1, NO
3 --N<40mgL
-1standard.
Claims (9)
1. a method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent, is characterized in that the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent is carried out according to the following steps:
One, cracking catalysis agent production waste water pH value is adjusted to 8.0 ~ 9.0, then carries out electricity flocculation;
Two, CANON technique, namely can be out of the water, and completes catalyst of cracking petroleum production wastewater treatment.
2. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, is characterized in that the flocculation of step one electricity adopts current density to be 25mAcm
-2direct current, polar plate spacing be 1.5cm.
3. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, is characterized in that the electric flocculation time of step one is 25min.
4. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, carries out aeration while it is characterized in that the flocculation of step one electricity.
5. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, is characterized in that the postprecipitation 30min of step one electricity flocculation.
6. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, it is characterized in that controlling dissolved oxygen in step 2 CANON technique is 0.5 ± 0.05mg/L, temperature of reaction is 30 ± 0.5 DEG C, pH value is 7.5 ~ 8.2, and hydraulic detention time is 15 ~ 20h.
7. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, it is characterized in that the expanded granular sludge bed EGSB of step 2 CANON technology utilization, the effective volume of reactor is 1.4L, and aspect ratio is 20.
8. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, is characterized in that step 2 CANON process reactor takes shading treatment.
9. the method for electricity flocculation-CANON combined treatment catalyst of cracking petroleum factory effluent according to claim 1, it is characterized in that step 2 CANON technique starting period inoculation CANON granule sludge, sludge concentration is 1.5gL
-1.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103172170A (en) * | 2013-03-08 | 2013-06-26 | 北京工业大学 | Sequencing batch completely autotrophic ammonia removal technology running method |
| CN103539323A (en) * | 2013-11-13 | 2014-01-29 | 东台市东方船舶装配有限公司 | Electric flocculation membrane bioreactor |
| US20140069864A1 (en) * | 2012-09-13 | 2014-03-13 | Hampton Roads Sanitation District | Method and apparatus for nitrogen removal in wastewater treatment |
| CN104609613A (en) * | 2014-12-26 | 2015-05-13 | 北京京润新技术发展有限责任公司 | Treatment device and treatment method for catalyst wastewater |
-
2015
- 2015-07-09 CN CN201510400190.0A patent/CN104909524A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20140069864A1 (en) * | 2012-09-13 | 2014-03-13 | Hampton Roads Sanitation District | Method and apparatus for nitrogen removal in wastewater treatment |
| CN103172170A (en) * | 2013-03-08 | 2013-06-26 | 北京工业大学 | Sequencing batch completely autotrophic ammonia removal technology running method |
| CN103539323A (en) * | 2013-11-13 | 2014-01-29 | 东台市东方船舶装配有限公司 | Electric flocculation membrane bioreactor |
| CN104609613A (en) * | 2014-12-26 | 2015-05-13 | 北京京润新技术发展有限责任公司 | Treatment device and treatment method for catalyst wastewater |
Non-Patent Citations (1)
| Title |
|---|
| 辛世希等: "电絮凝法处理催化剂高悬浮物污水试验研究", 《石油石化节能与减排》 * |
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