CN110357366A - Biochemical treatment method for Fischer-Tropsch synthesis wastewater - Google Patents
Biochemical treatment method for Fischer-Tropsch synthesis wastewater Download PDFInfo
- Publication number
- CN110357366A CN110357366A CN201910745027.6A CN201910745027A CN110357366A CN 110357366 A CN110357366 A CN 110357366A CN 201910745027 A CN201910745027 A CN 201910745027A CN 110357366 A CN110357366 A CN 110357366A
- Authority
- CN
- China
- Prior art keywords
- anaerobic reactor
- water
- aerobic tank
- buffer pool
- strain
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 100
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 59
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000011282 treatment Methods 0.000 title claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 238000010992 reflux Methods 0.000 claims abstract description 26
- 230000001376 precipitating effect Effects 0.000 claims abstract 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 144
- 239000010802 sludge Substances 0.000 claims description 66
- 239000007787 solid Substances 0.000 claims description 22
- 239000002253 acid Substances 0.000 claims description 17
- 241000894006 Bacteria Species 0.000 claims description 15
- 239000005416 organic matter Substances 0.000 claims description 14
- 230000015556 catabolic process Effects 0.000 claims description 13
- 238000006731 degradation reaction Methods 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 238000005273 aeration Methods 0.000 claims description 11
- 244000005706 microflora Species 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 10
- 230000000593 degrading effect Effects 0.000 claims description 9
- 239000008187 granular material Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 230000008021 deposition Effects 0.000 claims description 2
- 235000016709 nutrition Nutrition 0.000 claims description 2
- 238000004062 sedimentation Methods 0.000 claims description 2
- 230000003139 buffering effect Effects 0.000 claims 1
- 238000011081 inoculation Methods 0.000 claims 1
- 239000003513 alkali Substances 0.000 abstract description 10
- 238000006386 neutralization reaction Methods 0.000 abstract description 4
- 230000003851 biochemical process Effects 0.000 abstract description 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- 238000007599 discharging Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 8
- 238000004065 wastewater treatment Methods 0.000 description 6
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 241000589651 Zoogloea Species 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to a biochemical treatment process for Fischer-Tropsch synthesis reaction wastewater, and aims to provide a biochemical process capable of directly treating acidic Fischer-Tropsch synthesis wastewater, which can effectively reduce the COD value in the wastewater without adding alkali for neutralization. The treatment process flow is as follows: (1) discharging the Fischer-Tropsch synthesis wastewater into a buffer tank; (2) the effluent of the buffer tank enters a strain selector, and the device simultaneously receives the mixed liquid reflux of the facultative tank; (3) the effluent of the strain selector enters an anaerobic reactor; (3) treating the effluent of the anaerobic reactor; (4) part of mixed liquid in the aerobic tank flows back to the strain selector; (5) and precipitating the effluent of the aerobic tank. The process avoids adding alkali for neutralization, greatly reduces the treatment cost, and improves the stability of the flora through the strain selector.
Description
Technical field
Application field of the invention is Industrial Waste Water Treatments more particularly to F- T synthesis biochemical treatment process for wastewater, is applicable in
In the industrial wastewater for the strong feature high with concentration, acid that coal chemical industry Fischer-Tropsch synthesis generates.
Technical background
Coal chemical industry is the important industry in China, the use of coal is raw material, is converted into gas, liquid and solid product.Fischer-Tropsch
Synthesizing (Fischer-Tropsch synthesis) is one of important technology route of ICL for Indirect Coal Liquefaction, with a synthesis gas (oxidation
The mixed gas of carbon and hydrogen) it is raw material synthesizing liquid hydrocarbon mixture and oxygenatedchemicals under catalyst and felicity condition.It should
Process can generate the waste water that a large amount of concentration are high, acidity is strong, and COD (COD) concentration is about 15000~35000mg/L,
PH range is 2~4 or so.The general treatment process of such waste water, it usually needs add alkali adjustment pH be near neutral (Wu Jin is big etc.,
Treatment of Industrial Water, 2015,11:56-59；Tian Zhongming etc., water treatment technology, 2017,9:101-103), then reuse biochemical work
Skill (anaerobism, aerobic).When needing reuse waste water, generally along with film process (ultrafiltration, reverse osmosis) unit, recycling is biochemical
The water outlet of processing unit.The wastewater treatment process is not provided with strain selector, can not form the bacterium of suitable Fischer-Tropsch wastewater treatment
Group, cause the treatment process to have following prominent defect: 1) alkali charge is big, at high cost, because pH is lower, needs to add a large amount of alkali
PH can be adjusted as neutrality；2) reverse osmosis process energy consumption is high, adds the salt content that alkali improves waste water, increases osmotic pressure, improves
The energy consumption of reverse osmosis process；3) Net water recoveries are low, and strong brine yield is big, increase evaporator energy consumption；4) waste salt dregs yield is big,
Solidification disposal of waste is at high cost.Having its source in for the above problem adds alkali neutralization, and the present invention uses novel biochemical Processes and apparatus, by setting
Strain selector is set, filters out the specific flora of suitable Fischer-Tropsch wastewater treatment, without adding alkali that can handle Fischer-Tropsch synthetic wastewater, out
Water pH value is neutrality, and COD value is less than 100mg/L.
The present invention devises special flora selector, passes through on the basis of original F- T synthesis waste water treatment process
Acid waste water carries out environmental screening, carries out mechanical grading in conjunction with hydraulics and structure of reactor, ultimately forms acidproof anaerobic bacteria
Group carries out flora supplement to anaerobic reactor.The flora selector is closed cylindrical tank, and top is equipped with inclined plate separator
(or inclined plate sedimentation separator or sloping plate deposition separator), middle part are equipped with water distributor, and the method for operation is up flow type.As shown in Fig. 2,
Reactor top is cylindrical shape, and lower part is inverted conical shape (or rounding taper type).Returned sludge passes through the water inlet pipe of middle part side
Water distributor inside reacted device enters reactor, is formed by mud granule in mud mixed liquid and water formation along reactor
The inclined plate separator on centrifugal force difference and top, partial sludge sink to bottom, are discharged into subsequent anaerobic pond.Reactor head
Center (top of inclined plate separator) setting overflow device (depth be 0.5 meter) (or overflow launder), overflow device upper end liquid
The edge for flowing into end is zigzag.Waste water enters drainpipe by overflow device, and reactor is discharged.Specific design parameter is shown in that figure is got the bid
Note, other requirements are as follows: H/D=1.5~2.0, d/D=0.5.After the reflux of the mixed liquor of acid waste water and aerobic tank, from the bottom of positioned at
Portion's water distributor enters flora selector, acts on through hydraulic shear, discharges the anaerobic bacteria inside zoogloea.Mud mixture flows through
The solid-liquid separator in portion, bulky grain sludge are sunk by separation.Across the flora of solid-liquid separator, from top outflow flora selection
Device, as supplement strain, into anaerobic reaction system.
This discovery technical problems to be solved are how the method for anaerobism to be used directly to handle Fischer-Tropsch synthetic wastewater, avoided
Add alkali neutralization bring system problem, it is final to realize the mesh that the overall cost of F- T synthesis wastewater treatment and reuse is greatly reduced
's.
Summary of the invention
The present invention relates to a kind of F- T synthesis biochemical treatment process for wastewater, and the object of the present invention is to provide a kind of F- T synthesis
COD value in waste water can be effectively reduced in waste water low ph value biochemical processing process, the technique.
1. a kind of F- T synthesis biochemical treatment process for wastewater, processing technological flow are as follows:
(1) F- T synthesis waste water is discharged into buffer pool；(2) buffer pool water outlet enters strain selector, which connects simultaneously
Receive the reflux of oxygen compatibility pool mixed liquor；(3) strain selector water outlet enters anaerobic reactor；(3) it is carried out using anaerobic reactor water outlet
Processing；(4) aerobic tank part mixed liquor is back to strain selector；(5) aerobic tank water outlet is precipitated, is obtained remaining dirty
Mud, design parameter condition are as follows:
(1) by F- T synthesis waste water be sent into buffer pool, buffer pool collect waste water COD be in 5,000~25,000mg/L,
PH is 2.5~4.0, and temperature is 15~40 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/10 of anaerobic reactor
~1/4；It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
5~15%, aerobic tank using ordinary municipal domestic sludge be inoculated with, seed sludge amount be pond volume 20~30%, do not have to
Add extra nutritional object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/20 of aerobic tank inflow
~1/8；Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
(4) the strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria
Enter anaerobic reactor together with F- T synthesis waste water；
(5) anaerobic reactor utilizes the organic matter in the acidproof flora and other microflora degradation waste water in anaerobic reactor
Matter is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=2~8 day, and temperature is 32 DEG C~40 DEG C, leads to
Crossing flow of inlet water and residence time control total suspended solid content TSS is 5~10kg/m3；
(6) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, while the portion in aerobic tank
Mixed liquor is divided to flow back into strain selector, aerobic tank makes 2.0~4.0mg/L of dissolved oxygen in pond, hydraulic detention time by aeration
HRT=10~20h, temperature are 15 DEG C~30 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 1
~5kg/m3；
The pH value of waste water is maintained between 2.5~4.0 in the buffer pool.
Strain selector is set before anaerobic reactor, and effective volume is the 1/10~1/5 of anaerobic reactor.
Strain selector receives the reflux of aerobic tank mixed liquor, and regurgitant volume accounts for the 1/20~1/8 of inflow.
The A/O system forms special flora by strain selector, and COD volumetric loading design value is 0.20~
0.80kg/m3·d。
Outstanding feature of the invention has: 1) without adding alkali to adjust wastewater pH；2) flora selector is used, from denitrification sludge
The middle acidproof flora of separation and concentration, without persistently adding strain；3) acid waste water initially enters flora selector, subsequently into anaerobism
System.
Detailed description of the invention
Fig. 1 F- T synthesis biochemical treatment process for wastewater；
Fig. 2 strain selector structure schematic diagram.1, overflow device in figure；2, drainpipe；3, water inlet pipe；4, inclined plate separator,
5, sludge pipe.
Specific embodiment
Comparative example 1:
F- T synthesis waste water is discharged into buffer pool by a kind of F- T synthesis biochemical treatment process for wastewater, (1)；(2) buffer pool goes out
Water enters anaerobic reactor, is handled using anaerobic reactor buffer pool water outlet；(3) anaerobic reactor water outlet enters aerobic
Pond is handled anaerobic reactor water outlet using aerobic tank；(4) go out water mixed liquid to aerobic tank to precipitate, obtain remaining
Sludge and treated water body；
Its original processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 21,000mg/L, pH and is
3.5, temperature is 20 DEG C, and calcium oxide is added in buffer pool, makes to be discharged pH 7；
(2) buffer pool water outlet enters anaerobic reactor, anaerobic reactor using in anaerobic reactor acidproof flora and its
Organic substance in its microflora degradation waste water, is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=2
~8 days, temperature was 35 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 8kg/m3；
(3) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, and aerobic tank is made by aeration
Dissolved oxygen 3.0mg/L in pond, hydraulic detention time HRT=15h, temperature are 20 DEG C, are controlled by flow of inlet water and residence time
Total suspended solid content TSS is 3kg/m3；
(4) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 598mg/L, pH 7, TSS 30mg/L that aerobic tank pond, which is discharged COD,.
Embodiment 1
Between the buffer pool and anaerobic reactor of the F- T synthesis waste water biochemical treatment device described in the comparative example 1 of operation
One container is set as strain selector；Buffer pool water outlet enters strain selector, and strain selector receives aerobic tank simultaneously and goes out
The partial reflux water of water mixed liquid；The water outlet of strain selector enters anaerobic reactor；Aerobic tank part goes out water mixed liquid and is back to
Strain selector；
A kind of F- T synthesis biochemical treatment process for wastewater, processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 21,000mg/L, pH and is
3.5, temperature is 20 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/8 of anaerobic reactor；
It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
10%, aerobic tank is inoculated with using ordinary municipal domestic sludge, and seed sludge amount is the 20% of pond volume, without adding additional battalion
Support object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/12 of aerobic tank inflow；
Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
(4) the strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria
Enter anaerobic reactor together with F- T synthesis waste water；
(5) water outlet of strain selector enters anaerobic reactor, and anaerobic reactor utilizes the acidproof flora in anaerobic reactor
With the organic substance in other microflora degradation waste water, it is translated into biogas, anaerobic reactor condition is hydraulic detention time HRT
=2~8 days, temperature was 35 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 8kg/m3；
(6) anaerobic reactor, which is discharged, enters aerobic tank, the organic matter in further degrading waste water, while the pond A (aerobic tank)
In part mixed liquor flow back into strain selector, aerobic tank makes dissolved oxygen 3.0mg/L in pond, hydraulic detention time by aeration
HRT=15h, temperature are 20 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 3kg/m3；
(7) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 85mg/L, pH 6, TSS 20mg/L that aerobic tank pond, which is discharged COD,.Comparative example 2:
F- T synthesis waste water is discharged into buffer pool by a kind of F- T synthesis biochemical treatment process for wastewater, (1)；(2) buffer pool goes out
Water enters anaerobic reactor, is handled using anaerobic reactor buffer pool water outlet；(3) anaerobic reactor water outlet enters aerobic
Pond is handled anaerobic reactor water outlet using aerobic tank；(4) go out water mixed liquid to aerobic tank to precipitate, obtain remaining
Sludge and treated water body；
Its original processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 21,000mg/L, pH and is
3.5, temperature is 20 DEG C, and calcium oxide is added in buffer pool, makes to be discharged pH 7；
(2) buffer pool water outlet enters anaerobic reactor, anaerobic reactor using in anaerobic reactor acidproof flora and its
Organic substance in its microflora degradation waste water, is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=5
It, temperature is 30 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 6kg/m3；
(3) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, and aerobic tank is made by aeration
Dissolved oxygen 2.5mg/L in pond, hydraulic detention time HRT=18h, temperature are 25 DEG C, are controlled by flow of inlet water and residence time
Total suspended solid content TSS is 2kg/m3；
(4) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 714mg/L, pH 7, TSS 53mg/L that aerobic tank pond, which is discharged COD,.
Embodiment 2:
Between the buffer pool and anaerobic reactor of the F- T synthesis waste water biochemical treatment device described in the comparative example 2 of operation
One container is set as strain selector；Buffer pool water outlet enters strain selector, and strain selector receives aerobic tank simultaneously and goes out
The partial reflux water of water mixed liquid；The water outlet of strain selector enters anaerobic reactor；Aerobic tank part goes out water mixed liquid and is back to
Strain selector；
Its processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 21,000mg/L, pH and is
3.5, temperature is 20 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/ of anaerobic reactor
10；It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
15%, aerobic tank is inoculated with using ordinary municipal domestic sludge, and seed sludge amount is the 25% of pond volume, without adding additional battalion
Support object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/12 of aerobic tank inflow；
Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
(4) the strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria
Enter anaerobic reactor together with F- T synthesis waste water；
(5) water outlet of strain selector enters anaerobic reactor, and anaerobic reactor utilizes the acidproof flora in anaerobic reactor
With the organic substance in other microflora degradation waste water, it is translated into biogas, anaerobic reactor condition is hydraulic detention time HRT
=5 days, temperature was 30 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 6kg/m3；
(6) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, while the part in the pond A
Mixed liquor flows back into strain selector, and aerobic tank makes dissolved oxygen 2.5mg/L in pond, hydraulic detention time HRT=by aeration
18h, temperature are 25 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 2kg/m3；
(7) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 75mg/L, pH 6.5, TSS 18mg/L that aerobic tank pond, which is discharged COD,.Comparative example 3:
F- T synthesis waste water is discharged into buffer pool by a kind of F- T synthesis biochemical treatment process for wastewater, (1)；(2) buffer pool goes out
Water enters anaerobic reactor, is handled using anaerobic reactor buffer pool water outlet；(3) anaerobic reactor water outlet enters aerobic
Pond is handled anaerobic reactor water outlet using aerobic tank；(4) go out water mixed liquid to aerobic tank to precipitate, obtain remaining
Sludge and treated water body；
Its original processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 25,000mg/L, pH and is
3.2, temperature is 30 DEG C, and calcium oxide is added in buffer pool, makes to be discharged pH 7；
(2) buffer pool water outlet enters anaerobic reactor, anaerobic reactor using in anaerobic reactor acidproof flora and its
Organic substance in its microflora degradation waste water, is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=6
It, temperature is 32 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 7kg/m3；
(3) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, and aerobic tank is made by aeration
Dissolved oxygen 3.2mg/L in pond, hydraulic detention time HRT=18h, temperature are 27 DEG C, are controlled by flow of inlet water and residence time
Total suspended solid content TSS is 4kg/m3；
(4) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 625mg/L, pH 7, TSS 56mg/L that aerobic tank pond, which is discharged COD,.
Embodiment 3:
Between the buffer pool and anaerobic reactor of the F- T synthesis waste water biochemical treatment device described in the comparative example 3 of operation
One container is set as strain selector；Buffer pool water outlet enters strain selector, and strain selector receives aerobic tank simultaneously and goes out
The partial reflux water of water mixed liquid；The water outlet of strain selector enters anaerobic reactor；Aerobic tank part goes out water mixed liquid and is back to
Strain selector；
A kind of F- T synthesis biochemical treatment process for wastewater, processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 25,000mg/L, pH and is
3.2, temperature is 30 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/8 of anaerobic reactor；
It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
15%, aerobic tank is inoculated with using ordinary municipal domestic sludge, and seed sludge amount is the 25% of pond volume, without adding additional battalion
Support object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/15 of aerobic tank inflow；
Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
(4) the strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria
Enter anaerobic reactor together with F- T synthesis waste water；
(5) water outlet of strain selector enters anaerobic reactor, and anaerobic reactor utilizes the acidproof flora in anaerobic reactor
With the organic substance in other microflora degradation waste water, it is translated into biogas, anaerobic reactor condition is hydraulic detention time HRT
=6 days, temperature was 32 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 7kg/m3；
(6) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, while the part in the pond A
Mixed liquor flows back into strain selector, and aerobic tank makes dissolved oxygen 3.2mg/L in pond, hydraulic detention time HRT=by aeration
18h, temperature are 27 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 4kg/m3；
(7) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 78mg/L, pH 6.2, TSS 19mg/L that aerobic tank pond, which is discharged COD,.
Comparative example 4:
F- T synthesis waste water is discharged into buffer pool by a kind of F- T synthesis biochemical treatment process for wastewater, (1)；(2) buffer pool goes out
Water enters anaerobic reactor, is handled using anaerobic reactor buffer pool water outlet；(3) anaerobic reactor water outlet enters aerobic
Pond is handled anaerobic reactor water outlet using aerobic tank；(4) go out water mixed liquid to aerobic tank to precipitate, obtain remaining
Sludge and treated water body；
Its original processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 10,000mg/L, pH and is
2.8, temperature is 29 DEG C, and calcium oxide is added in buffer pool, makes to be discharged pH 7；
(2) buffer pool water outlet enters anaerobic reactor, anaerobic reactor using in anaerobic reactor acidproof flora and its
Organic substance in its microflora degradation waste water, is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=5
It, temperature is 36 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 9kg/m3；
(3) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, and aerobic tank is made by aeration
Dissolved oxygen 3.8mg/L in pond, hydraulic detention time HRT=20h, temperature are 28 DEG C, are controlled by flow of inlet water and residence time
Total suspended solid content TSS is 5kg/m3；
(4) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 697mg/L, pH 7, TSS 52mg/L that aerobic tank pond, which is discharged COD,.
Embodiment 4:
Between the buffer pool and anaerobic reactor of the F- T synthesis waste water biochemical treatment device described in the comparative example 4 of operation
One container is set as strain selector；Buffer pool water outlet enters strain selector, and strain selector receives aerobic tank simultaneously and goes out
The partial reflux water of water mixed liquid；The water outlet of strain selector enters anaerobic reactor；Aerobic tank part goes out water mixed liquid and is back to
Strain selector；
A kind of F- T synthesis biochemical treatment process for wastewater, processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 10,000mg/L, pH and is
2.8, temperature is 29 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/8 of anaerobic reactor；
It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
20%, aerobic tank is inoculated with using ordinary municipal domestic sludge, and seed sludge amount is the 20% of pond volume, without adding additional battalion
Support object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/9 of aerobic tank inflow；
Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
The strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria and
F- T synthesis waste water enters anaerobic reactor together；
(4) anaerobic reactor utilizes the organic matter in the acidproof flora and other microflora degradation waste water in anaerobic reactor
Matter is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=5 days, and temperature is 36 DEG C, passes through feed water flow
Amount and residence time control total suspended solid content TSS are 9kg/m3；
(5) water outlet of strain selector enters anaerobic reactor, and anaerobic reactor water outlet enters aerobic tank, and further degradation is useless
Organic matter in water, while the part mixed liquor in the pond A flows back into strain selector, aerobic tank makes dissolved oxygen in pond by aeration
3.8mg/L, hydraulic detention time HRT=20h, temperature are 28 DEG C, control total suspended solid by flow of inlet water and residence time
Content TSS is 5kg/m3；
(6) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 74mg/L, pH 6.1, TSS 16mg/L that aerobic tank pond, which is discharged COD,.
Embodiment 5:
A kind of F- T synthesis biochemical treatment process for wastewater, processing technological flow are as follows:
(1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 21,000mg/L, pH and is
3.5, temperature is 20 DEG C；
(2) between buffer pool and anaerobic reactor, strain selector is set, effective volume is the 1/8 of anaerobic reactor；
It is inoculated in anaerobic reactor using anaerobic expanded granular sludge bed (EGSB) granule sludge, seed sludge amount is inflow
10%, aerobic tank is inoculated with using ordinary municipal domestic sludge, and seed sludge amount is the 20% of pond volume, without adding additional battalion
Support object.
(3) the strain selector receives the mixed liquor reflux of aerobic tank simultaneously, and regurgitant volume accounts for the 1/12 of aerobic tank inflow；
Isolated acid fast bacteria and F- T synthesis waste water continuously enters anaerobic reactor together；
The strain selector receives buffer pool water outlet simultaneously, separates to acidproof flora；Isolated acid fast bacteria and
F- T synthesis waste water enters anaerobic reactor together；
(4) anaerobic reactor utilizes the organic matter in the acidproof flora and other microflora degradation waste water in anaerobic reactor
Matter is translated into biogas, and anaerobic reactor condition is hydraulic detention time HRT=2~8 day, and temperature is 35 DEG C, passes through water inlet
Flow and residence time control total suspended solid content TSS are 8kg/m3；
(5) water outlet of strain selector enters anaerobic reactor, and anaerobic reactor water outlet enters aerobic tank, and further degradation is useless
Organic matter in water, while the part mixed liquor in the pond A flows back into strain selector, aerobic tank makes dissolved oxygen in pond by aeration
3.0mg/L, hydraulic detention time HRT=15h, temperature are 20 DEG C, control total suspended solid by flow of inlet water and residence time
Content TSS is 3kg/m3；
(6) after stable operation 72h, mud-water separation is realized in aerobic tank water outlet, and a part of sludge reflux is to strain selector, separately
Aerobic tank is discharged in a part of sludge, and it is 85mg/L, pH 6, TSS 20mg/L that aerobic tank pond, which is discharged COD,.
Claims (6)
1. a kind of F- T synthesis biochemical procss for treating waste water, processing technological flow are that F- T synthesis waste water is discharged into buffering by (1)
Pond；(2) buffer pool water outlet enters anaerobic reactor, is handled using anaerobic reactor buffer pool water outlet；(3) anaerobic reaction
Device water outlet enters aerobic tank, is handled using aerobic tank anaerobic reactor water outlet；(4) go out water mixed liquid to aerobic tank to carry out
Precipitating obtains excess sludge and treated water body；It is characterized by:
A container is arranged between the buffer pool and anaerobic reactor of F- T synthesis waste water biochemical treatment device to select as strain
Device；Buffer pool water outlet enters strain selector, and strain selector receives the partial reflux water that aerobic tank goes out water mixed liquid simultaneously；Bacterium
Kind selector water outlet enters anaerobic reactor；Aerobic tank part goes out water mixed liquid and is back to strain selector；Carrying out practically parameter
Condition is as follows:
1) F- T synthesis waste water is sent into buffer pool, the COD that buffer pool collects waste water is in 5, and 000~25,000mg/L, pH are
2.5~4.0, temperature is 15~40 DEG C；
2) between buffer pool and anaerobic reactor, strain selector is set, volume is the 1/10~1/4 of anaerobic reactor；It should
The water mixed liquid that goes out that strain selector receives aerobic tank simultaneously flows back, and regurgitant volume accounts for the 1/20~1/8 of aerobic tank inflow；To resistance to
Sour flora is separated, and isolated acid fast bacteria and F- T synthesis waste water continuously enter anaerobic reactor together；
3) anaerobic reactor is using the organic substance in the acidproof flora and other microflora degradation waste water in anaerobic reactor, by it
It is converted into biogas, anaerobic reactor condition is hydraulic detention time HRT=2~8 day, and temperature is 32 DEG C~40 DEG C, passes through water inlet
Flow and residence time control total suspended solid content TSS are 5~10kg/m3；
4) anaerobic reactor water outlet enters aerobic tank, the organic matter in further degrading waste water, while the part in aerobic tank is mixed
It closes liquid and flows back into strain selector, aerobic tank makes 2.0~4.0mg/L of dissolved oxygen in pond, hydraulic detention time HRT=by aeration
10~20h, temperature are 15 DEG C~30 DEG C, and controlling total suspended solid content TSS by flow of inlet water and residence time is 1~5kg/
m3；
5) go out water mixed liquid to aerobic tank rest part to precipitate, obtain excess sludge and treated water body.
2. according to the method described in claim 1, it is characterized by: using anaerobic expanded granular sludge in the anaerobic reactor
Bed (EGSB) granule sludge inoculation, seed sludge amount are the 5~15% of inflow, and aerobic tank is connect using ordinary municipal domestic sludge
Kind, seed sludge amount is the 20~30% of pond volume, without adding extra nutritional object.
3. according to the method described in claim 1, it is characterized by: strain selector, effective body are arranged before anaerobic reactor
Product is the 1/10~1/5 of anaerobic reactor.
4. according to the method described in claim 1, it is characterized by: strain selector receives the reflux of aerobic tank mixed liquor, reflux
Amount accounts for the 1/20~1/8 of inflow.
5. according to the method described in claim 1, it is characterized by: the A/O system (it is anti-to specifically refer to buffer pool, anaerobism
Answer the system of device, strain selector and aerobic tank composition) special flora, the design of COD volumetric loading are formed by strain selector
Value is 0.20~0.80kg/m3·d。
6. according to the method described in claim 1, it is characterized by: the structure of the strain selector is closed cylindrical tank
Body, the intracorporal top of tank is equipped with inclined plate separator or inclined plate sedimentation separator or sloping plate deposition separator, the intracorporal middle part of tank are set
There is water distributor, the method for operation of strain selector is up flow type；Tank body top is cylindrical shape, lower part be hollow inverted conical shape or
Rounding taper type；The water distributor inside the reacted device of water inlet pipe that buffer pool water outlet and returned sludge pass through middle part side enters anti-
Device is answered, is separated by the inclined plate that mud granule in mud mixed liquid and water form the centrifugal force difference and top that are formed along reactor
Device, partial sludge sink to bottom, and another part is discharged into subsequent anaerobic reactor；The center of reactor head, tiltedly
The top setting overflow device or overflow launder of plate separator, the edge that overflow device upper end liquid flows into end is zigzag；Waste water passes through
Overflow device enters drainpipe, and reactor is discharged.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910745027.6A CN110357366B (en) | 2019-08-13 | 2019-08-13 | Biochemical treatment method for Fischer-Tropsch synthesis wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910745027.6A CN110357366B (en) | 2019-08-13 | 2019-08-13 | Biochemical treatment method for Fischer-Tropsch synthesis wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110357366A true CN110357366A (en) | 2019-10-22 |
| CN110357366B CN110357366B (en) | 2022-02-11 |
Family
ID=68224737
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910745027.6A Active CN110357366B (en) | 2019-08-13 | 2019-08-13 | Biochemical treatment method for Fischer-Tropsch synthesis wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110357366B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113735392A (en) * | 2021-10-08 | 2021-12-03 | 自然资源部第三海洋研究所 | Method for treating preserved fruit processing wastewater |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009059819A1 (en) * | 2007-11-09 | 2009-05-14 | Upm-Kymmene Oyj | Waste water treatment from a biomass-to-liquid process comprising synthesis gas production and integrated factory facility |
| CN101575159A (en) * | 2009-06-12 | 2009-11-11 | 哈尔滨工业大学 | Method of intensified denitrification and dephosphorization of urban sewage |
| US20110147313A1 (en) * | 2008-06-06 | 2011-06-23 | Eni S.P.A. | Process for the treatment of the aqueous stream coming from the fischer-tropsch reaction by means of ion exchange resins |
| CN103121754A (en) * | 2011-11-18 | 2013-05-29 | 上海市政工程设计研究总院（集团）有限公司 | Denitrification and dephosphorization technique |
| CN104556571A (en) * | 2014-12-25 | 2015-04-29 | 武汉凯迪工程技术研究总院有限公司 | Recycling treatment process and system for wastewater in Fischer-Tropsch synthesis reaction |
| CN105473514A (en) * | 2013-06-27 | 2016-04-06 | 沙索技术有限公司 | Production of biomass for use in the treatment of fischer-tropsch reaction water |
| CN105565491A (en) * | 2014-10-16 | 2016-05-11 | 中国石油化工股份有限公司 | Activated sludge treatment method and system for wastewater |
| CN105621613A (en) * | 2016-03-30 | 2016-06-01 | 刘晓涛 | A<2>/O nitrogen and phosphorus removal technology |
| CN105668780A (en) * | 2014-11-21 | 2016-06-15 | 中国寰球工程公司 | Acidification quick-recovery anaerobic reaction system |
| CN106946422A (en) * | 2017-05-23 | 2017-07-14 | 上海华畅环保设备发展有限公司 | Include the Cyclic Activated Sludge System sewage water treatment method and device of eddy flow processing |
| CN108285210A (en) * | 2018-02-02 | 2018-07-17 | 同济大学建筑设计研究院(集团)有限公司 | Integral type unpowered cyclone precipitates film filtering reactor |
| CN108911405A (en) * | 2018-07-26 | 2018-11-30 | 华电水务控股股份有限公司 | A kind of biochemical cell system and technique using five sections of bioanalysis |
-
2019
- 2019-08-13 CN CN201910745027.6A patent/CN110357366B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009059819A1 (en) * | 2007-11-09 | 2009-05-14 | Upm-Kymmene Oyj | Waste water treatment from a biomass-to-liquid process comprising synthesis gas production and integrated factory facility |
| US20110147313A1 (en) * | 2008-06-06 | 2011-06-23 | Eni S.P.A. | Process for the treatment of the aqueous stream coming from the fischer-tropsch reaction by means of ion exchange resins |
| CN101575159A (en) * | 2009-06-12 | 2009-11-11 | 哈尔滨工业大学 | Method of intensified denitrification and dephosphorization of urban sewage |
| CN103121754A (en) * | 2011-11-18 | 2013-05-29 | 上海市政工程设计研究总院（集团）有限公司 | Denitrification and dephosphorization technique |
| CN105473514A (en) * | 2013-06-27 | 2016-04-06 | 沙索技术有限公司 | Production of biomass for use in the treatment of fischer-tropsch reaction water |
| CN105565491A (en) * | 2014-10-16 | 2016-05-11 | 中国石油化工股份有限公司 | Activated sludge treatment method and system for wastewater |
| CN105668780A (en) * | 2014-11-21 | 2016-06-15 | 中国寰球工程公司 | Acidification quick-recovery anaerobic reaction system |
| CN104556571A (en) * | 2014-12-25 | 2015-04-29 | 武汉凯迪工程技术研究总院有限公司 | Recycling treatment process and system for wastewater in Fischer-Tropsch synthesis reaction |
| CN105621613A (en) * | 2016-03-30 | 2016-06-01 | 刘晓涛 | A<2>/O nitrogen and phosphorus removal technology |
| CN106946422A (en) * | 2017-05-23 | 2017-07-14 | 上海华畅环保设备发展有限公司 | Include the Cyclic Activated Sludge System sewage water treatment method and device of eddy flow processing |
| CN108285210A (en) * | 2018-02-02 | 2018-07-17 | 同济大学建筑设计研究院(集团)有限公司 | Integral type unpowered cyclone precipitates film filtering reactor |
| CN108911405A (en) * | 2018-07-26 | 2018-11-30 | 华电水务控股股份有限公司 | A kind of biochemical cell system and technique using five sections of bioanalysis |
Non-Patent Citations (1)
| Title |
|---|
| 李强等: "剩余活性污泥完全资源化利用微生物集成技术", 《微生物学通报》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113735392A (en) * | 2021-10-08 | 2021-12-03 | 自然资源部第三海洋研究所 | Method for treating preserved fruit processing wastewater |
| CN113735392B (en) * | 2021-10-08 | 2023-10-24 | 自然资源部第三海洋研究所 | Method for treating preserved fruit processing wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110357366B (en) | 2022-02-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Renou et al. | Landfill leachate treatment: Review and opportunity | |
| EP3392208B1 (en) | Bioreactor for treating sewage, sewage treatment system comprising the same and method of treating sewage | |
| US8758614B2 (en) | Anaerobic membrane bioreactor for treating a waste stream | |
| US20130134089A1 (en) | Method and system for treating wastewater | |
| US20080223783A1 (en) | High performance, energy efficient system and method for wastewater treatment with resource recovery and reduced residual solids generation | |
| US7547394B2 (en) | Wastewater treatment with aerobic granules | |
| WO2009124426A1 (en) | A method for treating pharmaceutical mixed wastewater in chemical industry park | |
| US9725346B2 (en) | Devices, systems and methods for facilitating nutrient removal by anaerobic ammonia oxidation | |
| CN105565581B (en) | Coal ethylene wastewater integrated conduct method | |
| CN110746036A (en) | Low-carbon-source sewage autotrophic denitrification deep denitrification device and method | |
| EP3265215B1 (en) | Systems and methods for treating dilute wastewater | |
| CN108083579B (en) | Modularized integrated system and process for treating non-fermented bean product production wastewater | |
| CN101781056B (en) | Treatment method of waste papermaking water | |
| CN103408201A (en) | Treatment method of industrial wastewater in silicon wafer mortar recovery | |
| CN201713415U (en) | Dye wastewater treatment device | |
| CN101781055B (en) | Treatment method of waste papermaking water | |
| CN109607786A (en) | A kind of combined anaerobic ammoxidation-anaerobism-membrane bioreactor sewage-treatment plant and method | |
| CN110357366A (en) | Biochemical treatment method for Fischer-Tropsch synthesis wastewater | |
| CN202148211U (en) | Treatment device of concentrated water generated by nano filtration and reverse osmosis membrane in garbage percolate treatment | |
| US20230121223A1 (en) | A Novel Single Hybrid Airlift Bioreactor for Wastewater Treatment | |
| CN102616997B (en) | Method for treating wastewater generated in production process of iron oxide pigment | |
| CN211521950U (en) | System for reducing concentration of pollutants in steel comprehensive wastewater | |
| US11447408B2 (en) | Combination of captivator and fixed film bioreactor solutions | |
| CN103288305B (en) | Slack coal pressure gasification wastewater recycling treatment method and treatment system as well as application | |
| CN211595353U (en) | High-efficient denitrogenation system of landfill leachate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |