CN1772652A - Technological process and apparatus of serial gas stripping inner circulation reactor - Google Patents
Technological process and apparatus of serial gas stripping inner circulation reactor Download PDFInfo
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- CN1772652A CN1772652A CNA2005101126722A CN200510112672A CN1772652A CN 1772652 A CN1772652 A CN 1772652A CN A2005101126722 A CNA2005101126722 A CN A2005101126722A CN 200510112672 A CN200510112672 A CN 200510112672A CN 1772652 A CN1772652 A CN 1772652A
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- stripping inner
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- 238000000034 method Methods 0.000 title description 16
- 230000008569 process Effects 0.000 title description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000010865 sewage Substances 0.000 claims abstract description 35
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 239000000523 sample Substances 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 110
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 19
- 239000001301 oxygen Substances 0.000 claims description 19
- 229910052760 oxygen Inorganic materials 0.000 claims description 19
- 238000005273 aeration Methods 0.000 claims description 12
- 238000006396 nitration reaction Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000005259 measurement Methods 0.000 claims description 11
- 230000004888 barrier function Effects 0.000 claims description 8
- 239000002351 wastewater Substances 0.000 claims description 7
- 238000013461 design Methods 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 12
- 241000894006 Bacteria Species 0.000 abstract description 8
- 239000005416 organic matter Substances 0.000 abstract description 3
- 241000108664 Nitrobacteria Species 0.000 abstract 1
- 230000000593 degrading effect Effects 0.000 abstract 1
- 238000012545 processing Methods 0.000 description 11
- 239000002957 persistent organic pollutant Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 4
- 230000036632 reaction speed Effects 0.000 description 4
- 208000019901 Anxiety disease Diseases 0.000 description 3
- 230000036506 anxiety Effects 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 244000005706 microflora Species 0.000 description 3
- 238000011017 operating method Methods 0.000 description 3
- 238000005842 biochemical reaction Methods 0.000 description 2
- 238000009395 breeding Methods 0.000 description 2
- 230000001488 breeding effect Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000005276 aerator Methods 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005755 formation reaction Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 238000001139 pH measurement Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000000306 recurrent effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The present invention belongs to the field of sewage biologically treating technology, and has two serially contained traditional gas stripping inner circulation reactors with gas conveyer, ORP probe, DO probe, pH probe and temperature probe; and liquid conveyer outside the lower reactor with pump and liquid pipeline to convey sewage into the lower reactor. The lower reactor is provided with sludge exhaust in the bottom, and water inlet and water exhaust on two sides; and the upper reactor has triphase separator with upper overflow weir to exhaust water, top gas exhaust, and water inlet and water exhaust on two sides. The present invention has suitable environment for both heterotrophic bacteria and nitrobacteria, raised organic matter degrading and nitrfication rate and low cost.
Description
Technical field
The present invention relates to a kind of biologic process for treating sewage method and device, contain the sewage of organic pollutant and ammonia nitrogen in order to processing.
Background technology
Gas stripping inner circulation reactor (Air-Lift Loop Bioreactor) is called for short ALBR, is a kind of novel, biological sewage treatment device efficiently.Dispose of sewage with it, have distinct advantages such as technical construction and form are simple, floor space is little, mass transfer biography oxygen performance is strong, sludge concentration is high, activity good, processing efficiency is high, operation scheme is flexible and changeable.Can in a reactor, remove common organic pollutant and ammonia nitrogen biochemical reaction processes such as (nitrifying processes) by controlling different operational conditionss, processing efficiency is higher, be applicable to and handle the land used anxiety, and water quality and quantity change greatly community wastewater and the trade effluent of continuous blow-down.Just because of above advantage, gas stripping inner circulation reactor develops very rapid at home and abroad, is the high-efficiency sewage treatment process of extensively promoting in the world at present, also is the nervous sub-district of land used and industrial enterprise's selection process.At present, the successful innovative gas stripping inner circulation reactor that will have of external environmental protection company is applied in the processing of various sewage, and has applied for relevant patent.At home, the various sewage works of application gas stripping inner circulation reactor technology are nearly hundred.
The operating procedure and the device synoptic diagram of tradition gas stripping inner circulation reactor technology are seen shown in Figure 1.Technological principle is: add a certain amount of tiny inert support or directly use active sludge in gas stripping inner circulation reactor, the bottom aeration causes upspout 1 and falls between the stream pipe 2 and certain gas holdup density difference occurs, thereby the mud that promotes liquid and mud or contain carrier circulates between managing 2 with falling to flow at upspout 1, most of mud or the mud that contains carrier are in recurrent state, minority mud or the mud that contains carrier are heavy than suspended sludge and water, so downward sedimentation is returned and fallen stream pipe 2 and continue to participate in circulating, water outlet and suspended sludge flow out from overflow weir.
The operating procedure of tradition Continuous Flow gas stripping inner circulation reactor technology is as follows:
(1) raw waste water continuously enters gas stripping inner circulation reactor by water pump 17 and carries out aeration aerating, sewage circulates in reactor, and the organism in the sewage fully contacts and effectively degraded with the interior various dominant microfloras efficiently of ammonia nitrogen and reactor;
(2) triphase separator 5 of disengaging zone is gas-liquid-solid three phase separation, wherein gas by the outlet of reactor upper top discharge, liquid is trapped afterwards Returning reactor by overflow weir 7 outflow reactors, solid (mud or contain the mud of carrier) and proceeds biochemical reaction.
As shown in Figure 1, traditional gas stripping inner circulation reactor technology is free-standing reactor.Organic degraded, nitration reaction all concentrate on upspout 1 and fall in the stream pipe 2 and carry out.In the aeration aerating stage, pressurized air is controlled by gas meter 14 through gas transmission pipeline 13, by aerating apparatus 12 gas is sent in the reactor at last.Simultaneously, reactor bottom also is provided with mud discharging mouth 8; Sidepiece is provided with water-in 9, water port 10 and water outlet 11.Organic matter degradation and ammonia nitrogen are nitrated to be finished by the diverse microbial population of two classes, is respectively aerobic heterotrophic bacterium and autotrophic type nitrifier.In traditional gas stripping inner circulation reactor technology, this two quasi-microorganism is in together in the reactor.When organic concentration was higher in the former water, the heterotrophic bacterium breeding was rapid, and surplus sludge volume strengthens, and sludge age shortens, thereby intensive has suppressed growth and the breeding of nitrifier, made that the nitrifier ratio in the active sludge descends.Simultaneously, in the measured response time, have only when organic pollutant concentration drops to lower level, nitrifier could with the competition of heterotrophic bacterium in occupy advantage, nitration reaction could be carried out fast.In addition,, tend to cause the nitration reaction deficiency of time, cause the water outlet ammonia nitrogen concentration not up to standard if reaction times control is improper.Therefore, although tradition gas stripping inner circulation reactor technology has certain advantage than traditional activated sludge process, but when handling the sewage of hardly degraded organic substance and ammonia nitrogen in high density, uncontrollable heterotrophic bacterium and nitrifier be in simultaneously the best living environment this to principal contradiction.Controlling improperly will influence effluent quality, reduces processing efficiency.
Traditional gas stripping inner circulation reactor structure if can be carried out the reasonable optimizing design, artificially two kinds of competitive floras are separated in gas stripping inner circulation reactor, not only can reach higher organism and ammonia nitrogen removal efficient, and can alleviate the actual engineering problem of land used anxiety.
Summary of the invention
The object of the present invention is to provide a kind of serial gas stripping inner circulation reactor processing method and the device that can effectively remove simultaneously organism and ammonia nitrogen in the sewage, can provide the suitableeest separately envrionment conditions for the growth of heterotrophism flora and nitrifying bacteria community, thereby significantly improve organic matter degradation rate and nitration reaction speed, under the prerequisite that guarantees effluent quality, increase substantially processing efficiency, save working cost, with solve organism and ammonia nitrogen concentration higher this to the principal contradiction in the sewage disposal.The structure of traditional gas stripping inner circulation reactor is carried out the actual engineering problem that the reasonably optimizing design can also be alleviated the land used anxiety.
Core technology scheme of the present invention is on the basis of original traditional gas stripping inner circulation reactor, one section gas stripping inner circulation reactor is set at an upper portion thereof again, and this process unit is that two section apparatus by gas stripping inner circulation reactor on the called after respectively and following gas stripping inner circulation reactor constitute.
Two reactors are arranged in series up and down, and each inside reactor structure is consistent with traditional gas stripping inner circulation reactor, by upspout 1, fall stream pipe 2, settling region 3 and bottom 4 formations.Each reactor all has separately independently triphase separator 5.
Upper and lower two sections gas stripping inner circulation reactors all are provided with air transporting arrangement.In the aeration aerating stage, pressurized air is provided by air compressor 15, through gas transfer pipeline 13, is controlled by gas meter 14, by aerating apparatus 12 gas is sent in the reactor at last.All place to gather redox potential (ORP) in upper and lower two reactors and be connected in measurement and control instrument 22 ORP probe 18, measure dissolved oxygen concentration (DO) and be connected in measurement and control instrument 23 DO probe 19, measure pH and be connected in the pH probe 20 of measurement and control instrument 24 and measure water temperature and be connected in the temp probe 21 of measurement and control instrument 25, the value of these four kinds of transmitters is respectively as the controlled variable of serial gas stripping inner circulation reactor technology operational process.
Side at following gas stripping inner circulation reactor is provided with liquid transporting apparatus, and sewage, is sent in the reactor through water-in 9 through liquid transmission pipelines 16 by pump 17; The bottom is provided with mud discharging mouth 8; Both sides are provided with water-in 9 and water port 10, and wherein water-in 9 is located at reactor lower part.
Triphase separator 5 tops in last gas stripping inner circulation reactor are provided with an overflow weir 7; Gas after triphase separator 5 separates is pooled in the gas barrier 6 of reactor head, and water outlet is discharged through overflow weir 7; Both sides are provided with water port 10 and water outlet 11, and wherein water outlet 11 is located at overflow weir 7 times.
The operating procedure of hardly degraded organic substance and realization nitration reaction is in the serial gas stripping inner circulation reactor removal sewage:
(1) raw waste water carries out aeration aerating through 17 pairs of following gas stripping inner circulation reactors of water pump, and the control gas-water ratio is higher than 1mg/L to guarantee the dissolved oxygen concentration (DO) in this section reactor.If the simple active sludge that uses should guarantee that then the interior sludge concentration of this section reactor is more than 4g/L; If add carrier in this section reactor, the volume that carrier bulk accounts for reactor should be controlled at 20%～50%.Mud in the reactor or carrier-containing mud are because upspout 1 and fall stream and manage the difference of the gas holdup between 2 and carry out cyclic motion, and microorganism on this stage carrier or the dominant microflora in the active sludge are mainly the aerobic heterotrophic bacterium of degradation of organic substances.Chemical oxygen demand (COD) (COD) design loading in this section reactor can be controlled in 3～15kg COD/kgMLVSSd.The pH of raw waste water should guarantee between 5～9.In the reaction process pH, dissolved oxygen concentration (DO), redox potential (ORP) and water temperature in the following gas stripping inner circulation reactor are monitored in real time, in time understood the operation conditions in the reactor.
(2) sewage after gas stripping inner circulation reactor is handled under the process enters gas stripping inner circulation reactor by behind the triphase separator 5 of this section; Gas then discharges from the gas barrier 6 at integral reactor top; Mud or the mud that contains carrier come back to down gas stripping inner circulation reactor, proceed circulating reaction.
(3) sewage that enters gas stripping inner circulation reactor is proceeded oxygenic aeration, and the control gas-water ratio is higher than 1mg/L to guarantee the dissolved oxygen concentration (DO) in this section reactor.If the simple active sludge that uses should guarantee that then the interior sludge concentration of this section reactor is more than 3g/L; If add carrier in this section reactor, its volume that accounts for this section reactor should be controlled at 20%～50%.Mud in this section reactor or the mud that contains carrier are because upspout 1 and fall stream and manage the difference of the gas holdup between 2 and carry out cyclic motion, and microorganism on this stage carrier or the dominant microflora in the active sludge are mainly nitrifier.Ammonia nitrogen design loading in this section reactor can be controlled in 1～5kg NH
4-N/kg MLVSSd.In the reaction process pH in the last gas stripping inner circulation reactor, dissolved oxygen concentration (DO), redox potential (ORP) and water temperature are monitored in real time, in time understood the operation conditions in the reactor.
(4) sewage after upward gas stripping inner circulation reactor is handled is after the triphase separator 5 on this section reactor top separates, and gas discharges from the gas barrier 6 of reactor head; Mud or the mud that contains carrier come back to gas stripping inner circulation reactor and proceed nitration reaction; Water outlet is then discharged whole reactor by overflow weir 7.
Contain a small amount of organism and a large amount of ammonia nitrogen in the above-mentioned sewage that enters in the gas stripping inner circulation reactor, by aeration aerating, mainly carry out nitration reaction, remaining organism also can further be degraded simultaneously.
The present invention can be widely used in containing the processing of the sewage of ammonia nitrogen in high density and Persistent organic pollutants, the clearance of organic pollutant, nitration reaction speed, total processing efficiency are significantly increased than traditional activated sludge process and traditional gas stripping inner circulation reactor, and system can steady in a long-term move.
Description of drawings:
Fig. 1 is the device synoptic diagram of traditional gas stripping inner circulation reactor processing method;
The isolated plant structural representation of Fig. 2 serial gas stripping inner circulation reactor processing method.
Among the figure: stream pipe 3-settling zone 4-bottom 5-three phase separator 6-gas release device 7-downflow weir 8-discharge pipeline 9-water inlet pipe 10-drainpipe 11-outlet pipe 12-aerator 13-gas transfer pipeline 14-gas flowmeter 15-air compressor 16-sewage transport pipeline 17-water pump 18-ORP probe 19-DO probe 20-pH probe 21-temp probe 22-ORP measurement and control instrument 23-DO analyzer 24-pH measurement and control instrument 25-temperature measurement-control instrument falls in 1-upspout 2-
Embodiment
Be described in further detail below in conjunction with 1,2 pairs of the specific embodiment of the present invention of accompanying drawing.
Serial gas stripping inner circulation reactor technology is made up of the gas stripping inner circulation reactor of two polyphones, respectively gas stripping inner circulation reactor and following gas stripping inner circulation reactor on the called after.Two reactor is communicated with by ring flange.
The serial gas stripping inner circulation reactor embodiment is as follows:
(1) raw waste water enters down through water pump 17 and carries out aeration aerating in the gas stripping inner circulation reactor, carries pressurized air by pneumatic line 13, and air flowmeter 14 pilot-gas flows, aerating apparatus 12 are evenly oxygen supply in reactor; Change by dissolved oxygen concentration in DO probe 19 and the DO measurement and control instrument 23 detection reaction processes; Water temperature changes in temp probe 21 and the temperature controller 25 assaying reaction devices.This stage dissolved oxygen concentration is controlled at more than the 1mg/L, and pH is controlled between 5～9.After gas stripping inner circulation reactor was handled down, the organic pollutant more than 90% was degraded by aerobic heterotrophic bacterium, contained a small amount of organism and a large amount of ammonia nitrogen in the residue sewage.
(2) by the sewage after down gas stripping inner circulation reactor is handled behind the triphase separator 5 of this section, enter gas stripping inner circulation reactor; Gas then discharges from the gas barrier 6 at whole tandem reactor top; Mud or the mud that contains carrier come back to down gas stripping inner circulation reactor and continue to participate in circulating reaction.
(3) sewage that enters gas stripping inner circulation reactor is proceeded oxygenic aeration, carries air by air delivery pipe road 13, and air flowmeter 14 pilot-gas flows, aerating apparatus 12 are evenly oxygen supply in reactor; Change by dissolved oxygen concentration in DO probe 19 and the DO measurement and control instrument 23 detection reaction processes; Water temperature changes in temp probe 21 and the temperature controller 25 assaying reaction devices, and this stage dissolved oxygen concentration is controlled at more than the 1mg/L.The further removal of in last gas stripping inner circulation reactor, having got back of the organism of handling back remaining 5%～10% through following gas stripping inner circulation reactor.Therefore, after serial gas stripping inner circulation reactor was handled, water outlet COD can reach emission request.The more important thing is that the ammonia nitrogen more than 95% is utilized and removed by nitrifier in last gas stripping inner circulation reactor.
(4) sewage after gas stripping inner circulation reactor is handled on the process is by behind the triphase separator 5 on this section top, and gas discharges from the gas barrier 6 of reactor upper top; Mud or the mud that contains carrier are got back to this section reactor again and are proceeded nitration reaction; Water outlet is then discharged whole reactor through overflow weir 7.
The sewage type that the present invention is suitable for is trade effluent and sanitary sewage.It is as follows to handle trade effluent water-in and water-out water quality condition: water inlet COD 2000～20000mg/L, BOD
51000～10000mg/L, ammonia nitrogen 50-300mg/L, TN 100～500mg/L, pH 5～9; Can reach through the water outlet after the high efficiency reactor processing: COD＜100mg/L, BOD
5＜50mg/L, ammonia nitrogen＜5mg/L, TN＜10mg/L, pH 6～8.Handle in the process of trade effluent, the COD load can reach 15kg COD/kg MLVSSd, and ammonia nitrogen loading can reach 5kg NH
4-N/kg MLVSSd.Concerning sanitary sewage, influent quality is: COD200～400mg/L, BOD
5100～300mg/L, ammonia nitrogen 50-100mg/L, TN 100～200mg/L, pH 6～8; Can reach through the water outlet after the high efficiency reactor processing: COD＜10mg/L, BOD
5＜5mg/L, ammonia nitrogen＜2mg/L, TN＜5mg/L, pH 6～8.Handle in the process of sanitary sewage, the COD load can reach 7kgCOD/kg MLVSSd, and ammonia nitrogen loading can reach 3kg ammonia nitrogen/kgMLVSSd.
Adopt the sewage of serial gas stripping inner circulation reactor art breading high-concentration hardly-degradable organic pollutant and ammonia nitrogen, the COD clearance reaches more than 95% after the steady running, and the average specific nitration reaction speed in the time of 30 ℃ reaches 0.70kg NH
4 +-N/ (kg MLSSd), water outlet can not detect ammonia nitrogen substantially, and effluent quality reaches national grade one discharge standard fully.COD clearance, nitration reaction speed, processing efficiency are significantly increased than traditional activated sludge process and traditional gas stripping inner circulation reactor technology.
Claims (2)
1, a kind of serial gas stripping inner circulation reactor, it is characterized in that, this reactor is on the basis of original traditional gas stripping inner circulation reactor, one section gas stripping inner circulation reactor two section apparatus is set at an upper portion thereof again constitutes, respectively gas stripping inner circulation reactor and following gas stripping inner circulation reactor on the called after;
Arranged in series about two reactors, each inside reactor structure is consistent with traditional gas stripping inner circulation reactor, includes upspout (1), falls stream pipe (2), settling region (3) and bottom (4); Each reactor all has separately independently triphase separator (5);
Upper and lower two sections gas stripping inner circulation reactors all are provided with existing air transporting arrangement; In the aeration aerating stage, pressurized air is provided by air compressor (15), through gas transfer pipeline (13), is controlled by gas meter (14), by aerating apparatus (12) gas is sent in the reactor at last; All place to gather redox potential ORP in upper and lower two reactors and be connected in measurement and control instrument (22) ORP probe (18), measure dissolved oxygen concentration DO and be connected in measurement and control instrument (23) DO probe (19), measure pH and be connected in the pH probe (20) and the mensuration water temperature of measurement and control instrument (24) and be connected in the temp probe (21) of measurement and control instrument (25);
Side at following gas stripping inner circulation reactor is provided with liquid transporting apparatus, and sewage, is sent in the reactor through water-in (9) through liquid transmission pipeline (16) by pump (17); The bottom is provided with mud discharging mouth (8); Both sides are provided with water-in (9) and water port (10), and wherein water-in (9) is located at reactor lower part;
Triphase separator in last gas stripping inner circulation reactor (5) top is provided with an overflow weir (7); Gas after triphase separator (5) separates is pooled to gas barrier (6) back at integral reactor top and discharges, and water outlet is discharged through overflow weir (7); Both sides are provided with water port (10) and water outlet (11), and wherein water outlet (11) is located under the overflow weir (7).
2, serial gas stripping inner circulation reactor processing method according to claim 1 is characterized in that, may further comprise the steps:
1). raw waste water carries out aeration aerating through water pump (17) to following gas stripping inner circulation reactor, and the control gas-water ratio is higher than 1mg/L to guarantee the dissolved oxygen concentration DO in this section reactor; If the simple active sludge that uses should guarantee that then the interior sludge concentration of this section reactor is more than 4g/L; If add the mud that contains carrier in this section reactor, the volume that volume accounts for reactor should be controlled at 20%～50%; Chemical oxygen demand COD design loading in this section reactor is controlled at 3～15kgCOD/kg MLVSSd; The pH of raw waste water is between 5～9; In the reaction process pH, dissolved oxygen concentration DO, redox potential (ORP) and water temperature in the following gas stripping inner circulation reactor are monitored in real time;
2). by behind the triphase separator (5) of this section, enter gas stripping inner circulation reactor through the sewage after gas stripping inner circulation reactor is handled down; Gas then discharges from the gas barrier (6) at integral reactor top; Mud or the mud that contains carrier come back to down gas stripping inner circulation reactor, proceed circulating reaction;
3). the sewage that enters gas stripping inner circulation reactor is proceeded oxygenic aeration, and the control gas-water ratio is higher than 1mg/L to guarantee the dissolved oxygen concentration DO in this section reactor; If the simple active sludge that uses should guarantee that then the interior sludge concentration of this section reactor is more than 3g/L; If add the mud that contains carrier in this section reactor, its volume that accounts for this section reactor is controlled at 20%50%; Ammonia nitrogen design loading in this section reactor is controlled at 1～5kg NH
4-N/kgMLVSSd; In the reaction process pH in the last gas stripping inner circulation reactor, dissolved oxygen concentration DO, redox potential ORP and water temperature are monitored in real time;
4). the sewage after upward gas stripping inner circulation reactor is handled is after the triphase separator (5) on this section reactor top separates, and gas discharges from the gas barrier (6) of reactor head; Mud or the mud that contains carrier come back to gas stripping inner circulation reactor and proceed nitration reaction; Water outlet is then discharged whole reactor by overflow weir (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101126722A CN1321919C (en) | 2005-10-14 | 2005-10-14 | Technological process and apparatus of serial gas stripping inner circulation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CNB2005101126722A CN1321919C (en) | 2005-10-14 | 2005-10-14 | Technological process and apparatus of serial gas stripping inner circulation reactor |
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| Publication Number | Publication Date |
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| CN1772652A true CN1772652A (en) | 2006-05-17 |
| CN1321919C CN1321919C (en) | 2007-06-20 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB2005101126722A Expired - Fee Related CN1321919C (en) | 2005-10-14 | 2005-10-14 | Technological process and apparatus of serial gas stripping inner circulation reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102023602A (en) * | 2010-11-03 | 2011-04-20 | 无锡金鑫集团有限公司 | Singlechip microcomputer control system special for device for biologically treating, circulating and recycling domestic sewage |
| CN102372360A (en) * | 2010-08-06 | 2012-03-14 | 李进民 | Biological sewage treatment device |
| CN106517671A (en) * | 2016-12-19 | 2017-03-22 | 天津大学 | Wastewater treating system suitable for high-cold and anoxic regions |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2458300Y (en) * | 2000-12-15 | 2001-11-07 | 北京环球绿洲科技有限公司 | Waste water treating final filtering tank |
| JP2002242899A (en) * | 2001-02-16 | 2002-08-28 | Inax Corp | Water supply device |
| CN2543952Y (en) * | 2001-05-08 | 2003-04-09 | 王崇达 | Filling type inner circulation biological reactor |
| CN1259124C (en) * | 2004-09-17 | 2006-06-14 | 清华大学 | Annular space gas lifting type loop reactor |
-
2005
- 2005-10-14 CN CNB2005101126722A patent/CN1321919C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102372360A (en) * | 2010-08-06 | 2012-03-14 | 李进民 | Biological sewage treatment device |
| CN102372360B (en) * | 2010-08-06 | 2013-10-16 | 李进民 | Biological sewage treatment device |
| CN102023602A (en) * | 2010-11-03 | 2011-04-20 | 无锡金鑫集团有限公司 | Singlechip microcomputer control system special for device for biologically treating, circulating and recycling domestic sewage |
| CN106517671A (en) * | 2016-12-19 | 2017-03-22 | 天津大学 | Wastewater treating system suitable for high-cold and anoxic regions |
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| Publication number | Publication date |
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| CN1321919C (en) | 2007-06-20 |
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